Method for producing catalyst composition for hydrogenation and catalyst composition for hydrogenation

ABSTRACT

A method for producing a catalyst composition for hydrogenation, wherein:
         (A): a titanocene compound represented by following general formula (1):       

     
       
         
         
             
             
         
       
         
         
           
             wherein R 5  and R 6  represent a group selected from the group consisting of hydrogen, a hydrocarbon group having 1 to 12 carbon atoms, an aryloxy group, an alkoxy group, a halogen group and a carbonyl group, and may be the same or different, and R 1  and R 2  represent a group selected from the group consisting of hydrogen and a hydrocarbon group having 1 to 12 carbon atoms, and may be the same or different, 
             provided that R 1  and R 2  represent are not all hydrogens or all hydrocarbon groups having 1 to 12 carbon atoms; 
             (B): a compound containing at least one element selected from the group consisting of elements Li, Na, K, Mg, Zn, Al, and Ca; and 
             (C): an unsaturated compound
 
are used, and
 
             the method has: 
             a force application step of applying a shearing force at a shearing rate of 1000 (1/s) or more to at least component (A); and 
             a step of mixing components (A), (B), and (C).

TECHNICAL FIELD

The present invention relates to a method for producing a catalystcomposition for hydrogenation and a catalyst composition forhydrogenation.

BACKGROUND ART

Conventionally, generally, a catalyst of a heterogeneous system and acatalyst of a homogeneous system are known as a catalyst forhydrogenation to be used in the step of hydrogenating an olefiniccompound.

Although the catalyst of the heterogeneous system generally isindustrially widely used, the catalyst of the heterogeneous system havelower activity than that of the latter catalyst of the homogeneoussystem and have the problem of being economically inefficient, becausethe catalysts of the heterogeneous system is required to be used at alarge amount for a desired hydrogenation reaction, and the reaction isat a high temperature and a high pressure.

On the other hand, since a hydrogenation reaction using the catalyst ofthe homogeneous system generally proceeds in a homogeneous system, thereare features that the catalyst of the homogeneous system have a higheractivity, require a lower amount of used catalyst, and are capable ofhydrogenation at a lower temperature and a lower pressure than thecatalyst of the heterogeneous system. However, the catalyst of thehomogeneous system have the drawbacks that the catalysts preparation iscomplex, the stability of the catalyst itself is low, reproducibilitiesare poor, and side reactions tend to occur. Moreover, the catalyst ofthe homogeneous system also have the problem that sufficient activity ofhydrogenation is not obtained when hydrogenating a alkyl-substitutedolefinic unsaturated double bond having a steric hindrance.

Accordingly, there is currently a strong need for the development of acatalyst of hydrogenation which has a high activity and which can behandled easily.

On the other hand, for a polymer containing an olefinic unsaturateddouble bond, although the unsaturated double bond is advantageouslyutilized in vulcanization and the like, due to this double bond, thepolymer also has drawbacks regarding poor stability, such as heatresistance and oxidation resistance. Such the drawback regarding poorstability is substantially improved by hydrogenating the polymer toremove the unsaturated double bonds in the polymer chain.

However, when hydrogenating the polymer, as compared with hydrogenatinga low-molecular-weight compound, the polymer is more easily affected bythe viscosity of the reaction system, steric hindrance of the polymerchain and the like, which makes hydrogenation more difficult. Inaddition, there is a problem that it is difficult to physically removeall the catalyst, after hydrogenation has finished. Therefore, there isa problem of causing filter clogging to an extruder used upon theproduction of a hydrogenated unsaturated double bond-containingcompound.

As described above, there has long been an issue for obtaining acatalyst composition for hydrogenation that is economically efficientnot to need to be used in a large amount, has a high storage stability,can exhibit sufficient activity of hydrogenation even when hydrogenatingolefinic unsaturated double bonds having a steric hindrance, and has alow degree of filter clogging in an extruder upon the production of ahydrogenated unsaturated double bond-containing compound.

Patent Literatures 1 and 2 disclose a method of hydrogenating anolefinic compound using a combination of a specific titanocene compoundand an alkyllithium; Patent Literatures 3 and 4 disclose a method ofhydrogenating an olefinic unsaturated (co)polymer using a combination ofa metallocene compound, with organic aluminum, organic zinc, organicmagnesium and the like; and Patent Literatures 5 and 6 disclose a methodof hydrogenating an olefinic unsaturated group-containing living polymerusing a combination of a specific titanocene compound and analkyllithium.

Moreover, Patent Literature 7 discloses a method of hydrogenating anolefinic double bond in an olefinic unsaturated double bond-containingpolymer using a combination of a specific titanocene compound and analkoxylithium. This method requires an expensive organic metal compoundother than alkoxylithium as a reductant.

Furthermore, Patent Literature 8 discloses a method of hydrogenating anolefinic unsaturated double bond-containing polymer using a combinationof a specific titanocene compound, an olefin compound, and a reductant.

Further, Patent Literature 9 discloses a method of hydrogenating anolefin compound using a combination of a metallocene compound having apentamethylcyclopentadienyl group, which is formed by substituting allof five hydrogens of a cyclopentadienyl group with methyl groups, and areductant.

Still further, Patent Literatures 10 and 11 disclose a method ofhydrogenating an olefin compound using a catalyst composition forhydrogenation comprising a specific titanocene compound, a reductant, anolefinic unsaturated double bond-containing polymer, and a polarcompound.

Still further, Patent Literature 12 discloses a method of hydrogenatingan olefin compound using a catalyst composition for hydrogenationcomprising a specific metallocene compound and a compound selected froma conjugated diene monomer, an acetylenic compound and an acetylenicmonomer.

CITATION LIST Patent Literature

-   Patent Literature 1: Japanese Patent Laid-Open No. 61-33132-   Patent Literature 2: Japanese Patent Laid-Open No. 1-53851-   Patent Literature 3: Japanese Patent Laid-Open No. 61-28507-   Patent Literature 4: Japanese Patent Laid-Open No. 62-209103-   Patent Literature 5: Japanese Patent Laid-Open No. 61-47706-   Patent Literature 6: Japanese Patent Laid-Open No. 63-5402-   Patent Literature 7: Japanese Patent Laid-Open No. 1-275605-   Patent Literature 8: Japanese Patent Laid-Open No. 2-172537-   Patent Literature 9: Japanese Patent Laid-Open No. 4-96904-   Patent Literature 10: Japanese Patent Laid-Open No. 08-33846-   Patent Literature 11: Japanese Patent Laid-Open No. 08-41081-   Patent Literature 12: Japanese Patent Laid-Open No. 2004-269665

SUMMARY OF INVENTION Technical Problem

However, in all of the above-described prior art techniques, sufficientproperties such as activity of hydrogenation, storage stability, and alow degree of filter clogging in an extruder upon production, have notyet been achieved.

Accordingly, it is an object of the present invention to provide amethod for producing a catalyst composition for hydrogenation, which iscapable of hydrogenating olefinic unsaturated double bond-containingcompounds (including polymers containing olefinic unsaturated doublebonds) with an economical advantage, and which has excellent storagestability, high activity of hydrogenation, and a low degree of filterclogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound.

Solution to Problem

As a result of intensive studies to solve the problems of the prior arttechniques, the present inventors have found that the problems in theabove-described prior art techniques can be solved by producing acatalyst composition for hydrogenation containing a predeterminedtitanocene compound (A), a compound containing a predetermined metalelement (B), and an unsaturated compound (C), under predeterminedconditions, thereby completing the present invention.

Namely, the present invention is as follows.

[1]

A method for producing a catalyst composition for hydrogenation,wherein:

(A): a titanocene compound represented by following general formula (1):

wherein R⁵ and R⁶ represent a group selected from the group consistingof hydrogen, a hydrocarbon group having 1 to 12 carbon atoms, an aryloxygroup, an alkoxy group, a halogen group, and a carbonyl group, and maybe the same or different, and R¹ and R² represent a group selected fromthe group consisting of hydrogen and a hydrocarbon group having 1 to 12carbon atoms, and may be the same or different,

provided that R¹ and R² are not all hydrogens or all hydrocarbon groupshaving 1 to 12 carbons;

(B): a compound containing at least one element selected from the groupconsisting of elements Li, Na, K, Mg, Zn, Al, and Ca; and

(C): an unsaturated compound

are used, and

the method comprises:

a force application step of applying a shearing force at a shearing rateof 1000 (1/s) or more to at least component (A); and

a step of mixing components (A), (B), and (C).

[2]

The method for producing the catalyst composition for hydrogenationaccording to [1] above, wherein the (C) is an unsaturated polymer (C1)having a fraction of an olefinic unsaturated double bond content of theside chains based on a total olefinic unsaturated double bond content is0.25 to 1.0.

[3]

The method for producing the catalyst composition for hydrogenationaccording to [1] above, wherein the (C) is an unsaturated compound (C2)having a molecular weight of 400 or less.

[4]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1] to [3] above, wherein the mass ratio of the(C) to the (A) ((C)/(A)) is set in a range of 0.1 to 8.

[5]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1] to [4] above, wherein the mass ratio of the(C) to the (A) ((C)/(A)) is set in a range of 0.1 to 4.

[6]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1], [2], [4], and [5] above, wherein

the (C) is an unsaturated polymer (C1) having a fraction of an olefinicunsaturated double bond content of the side chains based on a totalolefinic unsaturated double bond content is 0.25 to 1.0, and

the mass ratio of the (C1) and the (A) ((C1)/(A)) is set in a range of0.3 to 8.

[7]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1] to [6] above, comprises:

the step of mixing after the (A) and the (B), after the forceapplication step.

[8]

The method for producing the catalyst composition for hydrogenationaccording to [7] above, comprises:

the step of mixing after the (B) is added to a mixture of the (A) andthe (C), after the force application step.

[9]

The method for producing the catalyst composition for hydrogenationaccording to [8] above, comprises:

the step of mixing the (A), the (B), and the (C) after or during theforce application step of applying a shearing force at a shearing rateof 1000 (1/s) or more is applied to a mixture of the (A) and the (C).

[10]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1] to [9] above, further comprising a step ofmixing a polar compound (D), wherein

a mass ratio of the (D) and the (A) ((D)/(A)) is set in a range of 0.01to 2.

[11]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1] to [10] above, further comprising a step ofmixing a polar compound (D), wherein

a mass ratio of the (D) and the (A) ((D)/(A)) is set in a range of 0.01to 1.

[12]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1] to [11] above, wherein the (B) is an organiclithium compound.

[13]

The method for producing the catalyst composition for hydrogenationaccording to any one of [1] to [12] above, wherein a conjugated dienepolymer, or a copolymer formed of a conjugated diene and a vinylaromatic hydrocarbon is used as the unsaturated compound (C).

[14]

A catalyst composition for hydrogenation obtained by the method forproducing the catalyst composition for hydrogenation according to anyone of [1] to [13] above.

Advantageous Effects of Invention

According to the present invention, a method for producing a catalystcomposition for hydrogenation having high activity of hydrogenation bothat the initial stage of production and after storage thereof, excellentstorage stability, and a low degree of filter clogging in an extruderupon the production of a hydrogenated unsaturated double bond-containingcompound, can be provided.

DESCRIPTION OF EMBODIMENTS

An embodiment for carrying out the present invention (hereinafterreferred to as “present embodiment”) will be described in detail below.The present embodiment described below is an example for describing thepresent invention. The present invention is not limited to the followingcontent, and may be appropriately modified within the scope thereof.

[Method for Producing Catalyst Composition for Hydrogenation]

The method for producing a catalyst composition for hydrogenation of thepresent embodiment comprises using:

a titanocene compound (A) represented by the following general formula(1), following (B) and (C):

wherein R⁵ and R⁶ represent a group selected from the group consistingof hydrogen, a hydrocarbon group, an aryloxy group, an alkoxy group, ahalogen group and a carbonyl group, and may be the same or different,and R¹ and R² represent a group selected from the group consisting ofhydrogen and a hydrocarbon group having 1 to 12 carbon atoms, and may bethe same or different, provided that R¹ and R² are not all hydrogens orall hydrocarbon groups having 1 to 12 carbon atoms.

In formula (1), the hydrocarbon group having 1 to 12 carbon atomsrepresented by R¹, R², R⁵, and R⁶ includes, for example, a substituentrepresented by following general formula (2):

wherein R⁷ to R⁹ represent hydrogen or an alkyl hydrocarbon group having1 to 4 carbon atoms, provided that at least one of R⁷ to R⁹ is hydrogen;and n=0 or 1.

(B): a compound containing at least one element selected from the groupconsisting of elements Li, Na, K, Mg, Zn, Al, and Ca; and

(C): an unsaturated compound.

The method for producing a catalyst composition for hydrogenation of thepresent embodiment comprises a force application step of applying ashearing force at a shearing rate of 1000 (1/s) or more to at least the(A), and a step of mixing the (A), the (B), and the (C).

First, components used to produce a catalyst composition forhydrogenation of interest will be described.

(Component (A): Titanocene Compound)

Examples of component (A): a titanocene compound include, but are notlimited to, bis(η(5)-methylcyclopentadienyl)titanium dihydride,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dihydride,bis(η(5)-ethylcyclopentadienyl)titanium dihydride,bis(η(5)-propylcyclopentadienyl)titanium dihydride,bis(η(5)-n-butylcyclopentadienyl) titanium dihydride,bis(η(5)-methylcyclopentadienyl)titanium dimethyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dimethyl,bis(η(5)-ethylcyclopentadienyl)titanium dimethyl,bis(η(5)-propylcyclopentadienyl)titanium dimethyl,bis(η(5)-n-butylcyclopentadienyl) titanium dimethyl,bis(η(5)-methylcyclopentadienyl)titanium diethyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium diethyl,bis(η(5)-ethylcyclopentadienyl)titanium diethyl,bis(η(5)-propylcyclopentadienyl)titanium diethyl,bis(η(5)-n-butylcyclopentadienyl)titanium diethyl,bis(η(5)-methylcyclopentadienyl)titanium di-sec-butyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium di-sec-butyl,bis(η(5)-ethylcyclopentadienyl)titanium di-sec-butyl,bis(η(5)-propylcyclopentadienyl)titanium di-sec-butyl,bis(η(5)-n-butylcyclopentadienyl)titanium di-sec-butyl,bis(η(5)-methylcyclopentadienyl)titanium dihexyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dihexyl,bis(η(5)-ethylcyclopentadienyl)titanium dihexyl,bis(η(5)-propylcyclopentadienyl)titanium dihexyl,bis(η(5)-n-butylcyclopentadienyl)titanium dihexyl,bis(η(5)-methylcyclopentadienyl)titanium dioctyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dioctyl,bis(η(5)-ethylcyclopentadienyl)titanium dioctyl,bis(η(5)-propylcyclopentadienyl)titanium dioctyl,bis(η(5)-n-butylcyclopentadienyl)titanium dioctyl,bis(η(5)-methylcyclopentadienyl)titanium dimethoxide,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dimethoxide,bis(η(5)-ethylcyclopentadienyl)titanium dimethoxide,bis(η(5)-propylcyclopentadienyl)titanium dimethoxide,bis(η(5)-n-butylcyclopentadienyl)titanium dimethoxide,bis(η(5)-methylcyclopentadienyl)titanium diethoxide,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium diethoxide,bis(η(5)-ethylcyclopentadienyl)titanium diethoxide,bis(η(5)-propylcyclopentadienyl)titanium diethoxide,bis(η(5)-n-butylcyclopentadienyl) titanium diethoxide,bis(η(5)-methylcyclopentadienyl)titanium dipropoxide,bis(η(5)-dimethylcyclopentadienyl)titanium dipropoxide,bis(η(5)-ethylcyclopentadienyl)titanium dipropoxide,bis(η(5)-propylcyclopentadienyl)titanium dipropoxide,bis(η(5)-n-butylcyclopentadienyl) titanium dipropoxide,bis(η(5)-methylcyclopentadienyl)titanium dibutoxide,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dibutoxide,bis(η(5)-ethylcyclopentadienyl)titanium dibutoxide,bis(η(5)-propylcyclopentadienyl)titanium dibutoxide,bis(η(5)-n-butylcyclopentadienyl) titanium dibutoxide,bis(η(5)-methylcyclopentadienyl)titanium diphenyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium diphenyl,bis(η(5)-ethylcyclopentadienyl)titanium diphenyl,bis(η(5)-propylcyclopentadienyl)titanium diphenyl,bis(η(5)-n-butylcyclopentadienyl) titanium diphenyl,bis(η(5)-methylcyclopentadienyl)titanium di(m-tolyl),bis(η(5)-1,3-dimethylcyclopentadienyl)titanium di(m-tolyl),bis(η(5)-ethylcyclopentadienyl)titanium di(m-tolyl),bis(η(5)-propylcyclopentadienyl)titanium di(m-tolyl),bis(η(5)-n-butylcyclopentadienyl)titanium di(m-tolyl),bis(η(5)-methylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-1,3-methylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-ethylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-propylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-n-butylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-methylcyclopentadienyl)titanium di(m,p-xylyl),bis(η(5)-1,3-dimethylcyclopentadienyl)titanium di(m,p-xylyl),bis(η(5)-ethylcyclopentadienyl)titanium di(m,p-xylyl),bis(η(5)-propylcyclopentadienyl)titanium di(m,p-xylyl),bis(η(5)-n-butylcyclopentadienyl)titanium di(m,p-xylyl),bis(η(5)-methylcyclopentadienyl)titanium di(4-ethyl phenyl),bis(η(5)-1,3-dimethylcyclopentadienyl)titanium di(4-ethyl phenyl),bis(η(5)-ethylcyclopentadienyl)titanium di(4-ethyl phenyl),bis(η(5)-propylcyclopentadienyl)titanium di(4-ethyl phenyl),bis(η(5)-n-butylcyclopentadienyl)titanium di(4-ethyl phenyl),bis(η(5)-methylcyclopentadienyl)titanium di(4-hexyl phenyl),bis(η(5)-1,3-dimethylcyclopentadienyl)titanium di(4-hexyl phenyl),bis(η(5)-ethylcyclopentadienyl)titanium di(4-hexyl phenyl),bis(η(5)-propylcyclopentadienyl)titanium di(4-hexyl phenyl),bis(η(5)-n-butylcyclopentadienyl)titanium di(4-hexyl phenyl),bis(η(5)-methylcyclopentadienyl)titanium diphenoxide,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium diphenoxide,bis(η(5)-ethylcyclopentadienyl)titanium diphenoxide,bis(η(5)-propylcyclopentadienyl)titanium diphenoxide,bis(η(5)-n-butylcyclopentadienyl)titanium diphenoxide,bis(η(5)-n-butylcyclopentadienyl)titanium di(4-hexyl phenyl),bis(η(5)-methylcyclopentadienyl)titanium difluoride,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium difluoride,bis(η(5)-ethylcyclopentadienyl)titanium difluoride,bis(η(5)-propylcyclopentadienyl)titanium difluoride,bis(η(5)-n-butylcyclopentadienyl)titanium difluoride,bis(η(5)-methylcyclopentadienyl)titanium dichloride,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dichloride,bis(η(5)-ethylcyclopentadienyl)titanium dichloride,bis(η(5)-propylcyclopentadienyl)titanium dichloride,bis(η(5)-n-butylcyclopentadienyl) titanium dichloride,bis(η(5)-methylcyclopentadienyl)titanium dibromide,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dibromide,bis(η(5)-ethylcyclopentadienyl)titanium dibromide,bis(η(5)-propylcyclopentadienyl)titanium dibromide,bis(η(5)-n-butylcyclopentadienyl) titanium dibromide,bis(η(5)-methylcyclopentadienyl)titanium diiodide,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium diiodide,bis(η(5)-ethylcyclopentadienyl)titanium diiodide,bis(η(5)-propylcyclopentadienyl)titanium diiodide,bis(η(5)-n-butylcyclopentadienyl) titanium diiodide,bis(η(5)-methylcyclopentadienyl)titanium chloride methyl,bis(η(5)-di-1,3-methylcyclopentadienyl)titanium chloride methyl,bis(η(5)-ethylcyclopentadienyl)titanium chloride methyl,bis(η(5)-propylcyclopentadienyl)titanium chloride methyl,bis(η(5)-n-butylcyclopentadienyl)titanium chloride methyl,bis(η(5)-methylcyclopentadienyl) titanium chloride ethoxide,bis(η(5)-1,3-dimethylcyclopentadienyl) titanium chloride ethoxide,bis(η(5)-ethylcyclopentadienyl) titanium chloride ethoxide,bis(η(5)-propylcyclopentadienyl) titanium chloride ethoxide,bis(η(5)-n-butylcyclopentadienyl) titanium chloride ethoxide,bis(η(5)-methylcyclopentadienyl)titanium chloride phenoxaide,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium chloride phenoxaide,bis(η(5)-ethylcyclopentadienyl)titanium chloride phenoxaide,bis(η(5)-propylcyclopentadienyl)titanium chloride phenoxaide,bis(η(5)-n-butylcyclopentadienyl)titanium chloride phenoxaide,bis(η(5)-methylcyclopentadienyl)titanium dibenzyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dibenzyl,bis(η(5)-ethylcyclopentadienyl)titanium dibenzyl,bis(η(5)-propylcyclopentadienyl)titanium dibenzyl,bis(η(5)-n-butylcyclopentadienyl)titanium dibenzyl,bis(η(5)-methylcyclopentadienyl)titanium dicarbonyl,bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dicarbonyl,bis(η(5)-ethylcyclopentadienyl)titanium dicarbonyl,bis(η(5)-propylcyclopentadienyl)titanium dicarbonyl,bis(η(5)-n-butylcyclopentadienyl) titanium dicarbonyl.

These compounds may be used alone as one kind or in combination of twokinds or more.

The titanocene compound having these alkyl group-substitutedcyclopentadienyl groups is not limited to the above-described examples.Titanocene compounds other than those described above having two, three,or four alkyl group substituents on the cyclopentadienyl ring may alsobe preferably used.

Using the above-described various types of titanocene compounds, acatalyst composition for hydrogenation obtained by the production methodof the present embodiment hydrogenates the olefinic unsaturated doublebond of the olefinic compound (an olefinic unsaturated doublebond-containing compound; hereinafter also referred to as simply an“olefin compound”), and the catalyst composition for hydrogenation isalso excellent in heat resistance.

Especially, to obtain a catalyst composition for hydrogenation, whichhas a high activity of hydrogenating an olefinic unsaturated double bondof a conjugated diene polymer, or a copolymer formed of a conjugateddiene and a vinyl aromatic hydrocarbon, and which is capable ofhydrogenating the unsaturated double bond in a wide temperature range,preferred examples used as component (A): a titanocene compound includebis(η(5)-methylcyclopentadienyl)titanium dichloride,bis(η(5)-ethylcyclopentadienyl)titanium dichloride,bis(η(5)-propylcyclopentadienyl)titanium dichloride,bis(η(5)-n-butylcyclopentadienyl) titanium dichloride,bis(η(5)-methylcyclopentadienyl)titanium dimethyl,bis(η(5)-ethylcyclopentadienyl)titanium dimethyl,bis(η(5)-propylcyclopentadienyl)titanium dimethyl,bis(η(5)-n-butylcyclopentadienyl) titanium dimethyl,bis(η(5)-methylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-ethylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-propylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-n-butylcyclopentadienyl)titanium di(p-tolyl),bis(η(5)-methylcyclopentadienyl)titanium diphenyl,bis(η(5)-ethylcyclopentadienyl)titanium diphenyl,bis(η(5)-propylcyclopentadienyl)titanium diphenyl,bis(η(5)-n-butylcyclopentadienyl) titanium diphenyl.

Moreover, from the perspective of being stable handling in the air,preferred examples used as component (A): a titanocene compound includebis(η(5)-methylcyclopentadienyl)titanium dichloride,bis(η(5)-n-butylcyclopentadienyl) titanium dichloride,bis(η(5)-methylcyclopentadienyl)titanium diphenyl,bis(η(5)-n-butylcyclopentadienyl) titanium diphenyl,bis(η(5)-methylcyclopentadienyl)titanium di(p-tolyl), andbis(η(5)-n-butylcyclopentadienyl)titanium di(p-tolyl).

The above-described titanocene compound as component (A) can besynthesized, for example, by reacting a tetravalent titanocene halogencompound having a cyclopentadienyl group having an alkyl substituentwith with an aryl lithium.

The structure of the synthesized titanocene compound can be identifiedusing 1H-NMR and MS spectra.

((B): Compound Containing at Least One Element Selected from the GroupConsisting of Elements Li, Na, K, Mg, Zn, Al, and Ca)

As the above described (B) (hereinafter also referred to as a “compound(B),” a “component (B),” a “(B) component,” or “(B)”), among knownorganic metal compounds and metal-containing compounds that are capableof reducing above-described component (A), compounds containing at leastone element selected from the group consisting of elements Li, Na, K,Mg, Zn, Al, and Ca, are used.

Examples of component (B), but are not limited to, include an organiclithium compound, an organic sodium compound, an organic potassiumcompound, an organic zinc compound, an organic magnesium compound, anorganic aluminum compound, and an organic calcium compound.

These compounds may be used alone as one kind, or in combination of twokinds or more.

Examples of the organic lithium compound as component (B) include, butare not limited to, methyllithium, ethyllithium, n-propyllithium,isopropyllithium, n-butyllithium, sec-butyllithium, isobutyllithium,t-butyllithium, n-pentyllithium, n-hexyllithium, phenyllithium,cyclopentadienyllithium, m-tolyllithium, p-tolyllithium, xylyllithium,dimethylaminolithium, diethylaminolithium, methoxylithium,ethoxylithium, n-propoxylithium, isopropoxylithium, n-butoxylithium,sec-butoxylithium, t-butoxylithium, pentyloxylithium, hexyloxylithium,heptyloxylithium, octyloxylithium, phenoxylithium, 4-methylphenoxylithium, benzyloxylithium, 4-methyl benzyloxylithium.

Moreover, as component (B), a lithium phenolate compound obtained byreacting a phenolic stabilizer with the above described various types oforganic lithium can also be used.

Examples of the phenolic stabilizer include, but are not limited to,1-oxy-3-methyl-4-isopropyl benzene, 2,6-di-t-butylphenol,2,6-di-t-butyl-4-ethylphenol, 2,6-di-t-butyl-p-cresol,2,6-di-t-butyl-4-n-butylphenol, 4-hydroxymethyl-2,6-di-t-butylphenol,butyl hydroxyanisole, 2-(1-methylcyclohexyl)-4,6-dimethylphenol,2,4-dimethyl-6-t-butylphenol, 2-methyl-4,6-dinonylphenol,2,6-di-t-butyl-α-dimethyl amino-p-cresol,methylene-bis-(dimethyl-4,6-phenol),2,2′-methylene-bis-(4-methyl-6-t-butylphenol),2,2′-methylene-bis-(4-methyl-6-cyclohexylphenol),2,2′-methylene-bis-(4-ethyl-6-t-butylphenol),4,4′-methylene-bis-(2,6-di-t-butylphenol),2,2′-methylene-bis-(6-α-methyl-benzyl-p-cresol).

A particularly preferred example of the phenolic stabilizer is2,6-di-t-butyl-4-methylphenoxy lithium obtained by substituting with—OLi, the hydroxyl group of 2,6-di-t-butyl-p-cresolmethylphenoxy lithiumthat is the most common among the above described specific examples ofthe phenolic stabilizer.

Furthermore, examples of the organic lithium compound used as component(B) also include organic silicon lithium compounds such astrimethylsilyl lithium, diethylmethylsilyl lithium, dimethylethylsilyllithium, triethylsilyl lithium, and triphenylsilyl lithium, in additionto the above-described compounds.

Examples of the organic sodium compound used as component (B) include,but are not limited to, methyl sodium, ethyl sodium, n-propyl sodium,isopropyl sodium, n-butyl sodium, sec-butyl sodium, isobutyl sodium,t-butyl sodium, n-pentyl sodium, n-hexyl sodium, phenyl sodium,cyclopentadienyl sodium, m-tolyl sodium, p-tolyl sodium, xylyl sodium,and sodium naphthalene.

Examples of the organic potassium compound used as component (B)include, but are not limited to, methyl potassium, ethyl potassium,n-propyl potassium, isopropyl potassium, n-butyl potassium, sec-butylpotassium. isobutyl potassium, t-butyl potassium, n-pentyl potassium,n-hexyl potassium, triphenylmethyl potassium, phenyl potassium,phenylethyl potassium, cyclopentadienyl potassium, m-tolyl potassium,p-tolyl potassium, xylyl potassium, and potassium naphthalene

Examples of the organic magnesium compound used as component (B)include, but are not limited to, dimethyl magnesium, diethyl magnesium,dibutyl magnesium, ethylbutyl magnesium, methyl magnesium bromide, ethylmagnesium chloride, ethyl magnesium bromide, ethyl magnesium chloride,phenyl magnesium bromide, phenyl magnesium chloride, t-butyl magnesiumchloride, and t-butyl magnesium bromide.

Although component (B) may also be used as a living anionicpolymerization initiator of a conjugated diene compound and/or a vinylaromatic hydrocarbon compound, when an olefin compound, which is thetarget to be hydrogenated, is a conjugated diene polymer, or a copolymerformed of a conjugated diene and a vinyl aromatic hydrocarbon (a livingpolymer), having an active end of a metal contained in component (B),such an active end also acts as component (B).

Examples of the organic zinc compound used as component (B) include, butare not limited to, diethylzinc, bis(η(5)-cyclopentadienyl)zinc, anddiphenylzinc.

Examples of the organic aluminum compound used as component (B) include,but are not limited to, trimethyl aluminum, triethyl aluminum,triisobutyl aluminum, triphenyl aluminum, diethyl aluminum chloride,dimethyl aluminum chloride, ethyl aluminum dichloride, methyl aluminumsesquichloride, ethyl aluminum sesquichloride, diethyl aluminum hydride,diisobutyl aluminum hydride, triphenyl aluminum, andtri(2-ethylhexyl)aluminum, (2-ethylhexyl)aluminum dichloride, methylaluminoxane, and ethyl aluminoxane.

In addition to these, alkali (earth) metal hydrides such as lithiumhydride, potassium hydride, sodium hydride, and calcium hydride; andhydrides containing two or more types of metals, such as sodium aluminumhydride, potassium aluminum hydride, diisobutyl sodium aluminum hydride,tri(t-butoxy)aluminum hydride, triethyl sodium aluminum hydride,diisobutyl sodium aluminum hydride, triethyl sodium aluminum hydride,triethoxy sodium aluminum hydride, and triethyl lithium aluminumhydride, can also be used as component (B).

Moreover, a complex synthesized by reacting in advance the abovedescribed organic alkali metal compound with the organic aluminumcompound, a complex synthesized by reacting in advance the organicalkali metal compound with the organic magnesium compound (ate complex),and the like can also be used as component (B).

From the perspective of a high activity of hydrogenation, the organicmetal compound and metal-containing compound as component (B) arepreferably compounds containing Li or Al.

Preferred examples of the compound containing Li or Al include triethylaluminum, triisobutyl aluminum, sec-butyl lithium, and n-butyl lithium.

From the perspective of the activity of hydrogenation of a catalystcomposition for hydrogenation at the initial stage of production andafter storage thereof, and a low degree of filter clogging in anextruder upon the production of a hydrogenated unsaturated doublebond-containing compound, an organic lithium compound is morepreferable.

((C): Unsaturated Compound)

The (C) that is an unsaturated compound (hereinafter also referred to as“(C) an unsaturated compound,” a “(C) component,” a “component (C),” or“(C)”) is a compound having at least one unsaturated group in a moleculethereof.

In the present embodiment, from the perspective of the capability ofhydrogenating an olefinic unsaturated double bond-containing compoundwith economical advantage, and the capability of producing a polymerhaving excellent storage stability, good feed properties, and excellentcolorlessness by a hydrogenating step, component (C) that is anunsaturated compound is preferably an unsaturated polymer (C1)(hereinafter also referred to as “(C1) an unsaturated polymer, a “(C1)component,” a “component (C1),” or “(C1)”), having a fraction of anolefinic unsaturated double bonds content of the side chains based on atotal olefinic unsaturated double bond content of 0.25 to 1.0.

Moreover, as described later, from the perspective of the capability ofhydrogenating an olefinic unsaturated double bond-containing compound(including a polymer containing an olefinic unsaturated double bond)with economical advantage, and the capability of producing a polymerhaving excellent storage stability, good feed properties, and excellentcolorlessness by a hydrogenating step, component (C) that is anunsaturated compound is also preferably an unsaturated compound (C2)(hereinafter also referred to as “(C2) an unsaturated compound,” a “(C2)component,” a “component (C2),” or “(C2)”) having a molecular weight of400 or less which has one or more unsaturated groups in a moleculethereof.

Component (C) that is an unsaturated compound can be produced using theafter-described predetermined monomer, and component (C1) that is anunsaturated polymer can be produced by polymerizing the after-describedpredetermined monomer.

Examples of the above described monomer include a conjugated diene, andgenerally include a conjugated dienes having 4 to about 12 hydrocarbons.

Examples of the monomer include, but are not limited to, 1,3-butadiene,isoprene, 2,3-dimethylbutadiene, 1,3-pentadiene,2-methyl-1,3-pentadiene, 1,3-hexadiene, 4,5-diethyl-1,3-octadiene, and3-butyl-1,3-octadiene.

These may be polymerized alone or copolymerized in combinations of twoor more. Among these, 1,3-butadiene and isoprene are preferable becausethey can produce component (C1) in an industrially large scale and arerelatively easily handled. Homopolymers or copolymers formed of thesemonomers, such as polybutadiene, polyisoprene, and a butadiene/isoprenecopolymer, are preferable.

Furthermore, a polymer obtained by singly polymerizing norbornadiene,cyclopentadiene, 2,3-dihydrodicyclopentadiene, and an alkyl-substitutedproduct thereof or by copolymerizing two or more of these substances incombination, may also be used.

From the perspective of increasing the fraction of an olefinicunsaturated double bond content of the side chains, component (C1) thatis an unsaturated polymer is preferably a conjugated diene polymer, or acopolymer formed of the above described conjugated diene and an aromaticvinyl compound.

Examples of the aromatic vinyl compound include styrene, t-butylstyrene,α-methylstyrene, p-methylstyrene, divinylbenzene, 1,1-diphenylethylene,and N,N-diethyl-p-aminoethylstyrene. Among others, styrene isparticularly preferable.

The most preferred examples of the specific copolymer include abutadiene/styrene copolymer and an isoprene/styrene copolymer.

These copolymers may be in any form such as random, block, star-shapedblock, tapered block and the like, and are not particularly limited.

When component (C1) that is an unsaturated polymer is a copolymer formedof a conjugated diene and an aromatic vinyl compound, the amount of thearomatic vinyl compound bound is preferably 70% by mass or less.

Component (C1) that is an unsaturated polymer may have a functionalgroup such as a hydroxyl group, a carboxyl group, an amino group, or anepoxy group.

From the perspective of the activity of hydrogenation, handling, feedproperties, and storage stability of the catalyst composition forhydrogenation of the present embodiment, the number average molecularweight of component (C1) that is an unsaturated polymer is preferablymore than 400, and more preferably 500 or more, and from the perspectiveof handling, it is preferably 1,000,000 or less.

The number average molecular weight of component (C1) is more preferably500 or more and 20,000 or less, even more preferably 800 or more and15,000 or less, and further preferably 1,000 or more and 10,000 or less.

The number average molecular weight of the component (C1) (a value interms of polystyrene) can be measured by GPC (gel permeationchromatography).

It is to be noted that the term “good feed properties” refers to whenfeeding a catalyst composition for hydrogenation via a predeterminedpipe, after storing the catalyst composition for a certain period oftime under a predetermined environment, the ability to continuouslymaintain a smooth feed state without clogging of the pipe.

Moreover, the term “good handling” refers to a low viscosity when insolution, high mixing properties and rate of transfer, and lowsusceptibility of adherence to the equipment, the pipe, etc.

From the perspective of the activity of hydrogenation, handling(lowering viscosity of a solution), and storage stability regarding feedproperties, of the catalyst composition for hydrogenation produced bythe production method of the present embodiment, and a low degree offilter clogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound, the fraction of an olefinicunsaturated double bond content of the side chains based on a totalolefinic unsaturated double bond content is preferably 0.25 to 1.0 incomponent (C1) that is an unsaturated polymer.

The fraction of an olefinic unsaturated double bond content of the sidechains based on a total olefinic unsaturated double bond content isdefined as X═Y/Z, wherein

“the fraction of an olefinic unsaturated double bond of the side chainsbased on total olefinic unsaturated double bond” represents X,

[the number of olefinic unsaturated carbon/carbon double bonds of theside chains of a component polymer], and represents Y, and

[the total number of olefinic unsaturated carbon/carbon double bonds ofa component polymer] represents Z,

The value of X is preferably in a range of 0.25 to 1.0.

This value range means that when polybutadiene is used as a specificexample of component (C1) that is an unsaturated polymer, the fractionof an olefinic unsaturated double bond content of the side chains (1,2bonds) based on a total olefinic unsaturated double bond content (cis1,4 bond, trans 1,4 bond, and 1,2 bond) is in a range of 0.25 to 1 (25to 100 mol %).

The above described X is more preferably in a range of 0.40 to 1.0, evenmore preferably in a range of 0.50 to 0.95, and further preferably in arange of 0.60 to 0.95.

The above described X that is the fraction of a olefinic unsaturateddouble bond content of the side chains based on a total olefinicunsaturated double bond content can be measured using NMR.

The mass ratio of above described component (C1) (an unsaturatedcompound) to above described component (A) (a titanocene compound),(C1)/(A), is preferably 0.1 or more and 8 or less.

From the perspective of the activity of hydrogenation, handling, andstorage stability regarding feed properties, of the catalyst compositionfor hydrogenation produced by the production method of the presentembodiment, the mass ratio of above described component (C1) (anunsaturated polymer) to above described component (A) (a titanocenecompound), (C1)/(A), is preferably 0.1 or more, and more preferably 0.3or more. From the perspective of storage stability regarding feedproperties, economical efficiency, and further, suppression of theyellowing of a hydrogenated polymer that has been hydrogenated with thecatalyst composition for hydrogenation, the mass ratio ((C1)/(A)) ispreferably 8 or less, more preferably 4 or less, even more preferably 3or less, and further preferably 2 or less.

The mass ratio of (C1) to (A) ((C1)/(A)) is more preferably in a rangeof 0.4 to 5, even more preferably in a range of 0.5 to 3, and furtherpreferably in a range of 0.7 to 2.

Moreover, from the perspective of the activity of hydrogenation,handling (low viscosity), and storage stability regarding feedproperties, of the catalyst composition for hydrogenation produced bythe production method of the present embodiment, the total olefinicunsaturated double bond content (mol) of the side chains in component(C1) as a whole that is an unsaturated polymer per mol of component (A)that is a titanocene compound is preferably 0.3 mol or more, and fromperspective of suppression of the yellowing of the polymer, it ispreferably 30 mol or less. Furthermore, it is more preferably in a rangeof 0.5 mol to 20 mol, even more preferably in a range of 1.0 mol to 15mol, and further preferably in a range of 2.0 mol to 12 mol.

In the present embodiment, from the perspective of the capability ofhydrogenating an olefinic unsaturated double bond-containing compound(including a polymer containing an olefinic unsaturated double bond)with economical advantage, and the capability of producing a polymerhaving excellent storage stability, good feed properties, and excellentcolorlessness by a hydrogenating step, as described above, a compound(C2) (hereinafter also referred to as “(C2) an unsaturated compound,” a“(C2) component,” a “component (C2),” or “(C2)”) that has a molecularweight of 400 or less and has one or more unsaturated groups in amolecule thereof, can also preferably used as component (C) that is anunsaturated compound.

From the perspective of feed properties after the storage of thecatalyst composition for hydrogenation, component (C2) has a molecularweight of 400 or less, and the molecular weight is preferably 300 orless, more preferably 200 or less, and further preferably 150 or less.

Component (C2) that is an unsaturated compound may be produced bypolymerizing a predetermined monomer.

Examples of the above described monomer include, but are not limited to,conjugated dienes generally having 4 to about 12 hydrocarbons, such as1,3-butadiene, isoprene, 2,3-dimethylbutadiene, 1,3-pentadiene,2-methyl-1,3-pentadiene, 1,3-hexadiene, 4,5-diethyl-1,3-octadiene or3-butyl-1,3-octadiene, monoterpene, a vinyl aromatic compound,norbornadiene, cyclopentadiene, cyclohexadiene,2,3-dihydrodicyclopentadiene, and acetylenes.

These compounds may be used alone as one kind, or two kinds or more ofthese compounds may be used in combination and also may be copolymerizedwith one another.

From the perspective of the activity of hydrogenation of a catalystcomposition for hydrogenation obtained by the method for producing acatalyst composition for hydrogenation of the present embodiment at theinitial stage of production and after storage thereof, and a low degreeof filter clogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound, the amount of unsaturatedgroups in unsaturated compound (C2) has a preferred range.

Specifically, from the perspective of the activity of hydrogenation of acatalyst composition for hydrogenation at the initial stage ofproduction and after storage thereof, and a low degree of filterclogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound, the amount of unsaturatedgroups in 1 mol of component (C2) is preferably 2 mol or more. On theother hand, from the perspective of the activity of hydrogenation andfeed properties of a catalyst composition for hydrogenation at theinitial stage of production and after storage thereof, a low degree offilter clogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound, and suppression of theyellowing of the polymer of a hydrogenated olefin compound, it is in arange of 5 mol or less. The amount of unsaturated groups in 1 mol ofcomponent (C2) is more preferably in a range of 2 mol or more and 4 molor less, even more preferably in a range of 2 mol or more and 3 mol orless, and further preferably 3 mol.

The amount of unsaturated groups in the (C2) can be measured using NMR.

From the perspective of the activity of hydrogenation, handling, andstorage stability regarding feed properties of the catalyst compositionfor hydrogenation produced by the production method of the presentembodiment, the mass ratio between component (C2) (an unsaturatedcompound) and component (A) (a titanocene compound) ((C2)/(A)) ispreferably 0.1 or more. On the other hand, from the perspective ofstorage stability regarding feed properties, economical efficiency, andfurther, suppression of the yellowing of a hydrogenated polymer that hasbeen hydrogenated with the above described catalyst composition forhydrogenation, the mass ratio ((C2)/(A)) is preferably 8.0 or less.

From the perspective of the activity of hydrogenation, handling, storagestability regarding feed properties, and economical efficiency of theproduced catalyst composition for hydrogenation, and suppression of theyellowing of a hydrogenated polymer, the mass ratio of (C2) and (A)(=(C2)/(A)) is preferably in a range of 0.1 to 8, more preferably in arange of 0.1 to 4, even more preferably in a range of 0.5 to 3, andfurther preferably in a range of 1.0 to 2.5.

As described above, by using an unsaturated compound (C2) having amolecular weight of 400 or less as an unsaturated compound (C), thecatalyst composition for hydrogenation produced by the production methodof the present embodiment has excellent storage stability, good feedproperties, and excellent feed properties even after the storagethereof.

In addition, by setting the amount of unsaturated groups in (C2) in theabove-described range based on the molar ratio of (C2) to component (A),the amount of hydrogen added to those other than the olefinicunsaturated double bonds in the polymer as a target to be hydrogenatedcan be reduced, and as a result, high activity of hydrogenation can beobtained.

(Component (D): Polar Compound)

From the perspective of high activity of hydrogenation at the initialstage of production and after storage, and reduction in filter cloggingin an extruder upon the production of a hydrogenated unsaturated doublebond-containing compound, it is preferable to further add the followingcomponent (D) that is a polar compound (hereinafter also referred to asa “polar compound (D),” a “(D) component,” or “D”) in the method forproducing a catalyst composition for hydrogenation of the presentembodiment.

Component (D) that is a polar compound is a compound having N, O or S.Examples of component (D) include an alcohol compound, an ethercompound, a thioether compound, a ketone compound, a sulfoxide compound,a carboxylic acid compound, a carboxylate compound, an aldehydecompound, a lactam compound, a lactone compound, an amine compound, anamide compound, a nitrile compound, an epoxy compound, and an oximecompound.

Specific examples of these polar compounds are given below.

Examples of the alcohol compound include, but are not limited to,monohydric alcohols such as methyl alcohol, ethyl alcohol, propylalcohol, n-butyl alcohol, sec-butyl alcohol, isobutyl alcohol,tert-butyl alcohol, n-amyl alcohol, iso-amyl alcohol, hexyl alcohol andan isomer thereof, heptyl alcohol and an isomer thereof, octyl alcoholand an isomer thereof, capryl alcohol, nonyl alcohol and an isomerthereof, decyl alcohol and an isomer thereof, benzyl alcohol, phenol,cresol and 2,6-di-tert-butyl-p-cresol, and dihydric alcohols such asethylene glycol, propylene glycol, butanediol, pentyl glycol, hexylglycol, heptyl glycol, and glycols that are isomers of these alcohols.Moreover, trihydric alcohol such as glycerin, or alcohol compoundshaving another functional group in a single molecule thereof, such asethanolamine or glycidyl alcohol, may also be used.

Examples of the ether compound include, but are not limited to, dimethylether, diethyl ether, di-n-propyl ether, diisopropyl ether, di-n-butylether, di-sec-butyl ether, diphenyl ether, methylethyl ether, ethylbutylether, butylvinyl ether, anisole, ethylphenyl ether, ethylene glycoldimethyl ether, ethylene glycol diethyl ether, ethylene glycol dibutylether, diethylene glycol dimethyl ether, diethylene glycol diethylether, furan, tetrahydrofuran, α-methoxy tetrahydrofuran, pyran,tetrahydropyran, and dioxane.

Moreover, a compound having another functional group in a moleculethereof, such as tetrahydrofurancarboxylic acid, may also be used.

Examples of the thioether compound include, but are not limited to,dimethyl sulfide, diethyl sulfide, di-n-butyl sulfide, di-sec-butylsulfide, di-tert-butyl sulfide, diphenyl sulfide, methyl ethyl sulfide,ethyl butyl sulfide, thioanisole, ethyl phenyl sulfide, thiophene, andtetrahydrothiophene.

Examples of the ketone compound include, but are not limited to,acetone, diethyl ketone, di-n-propyl ketone, diisopropyl ketone,di-n-butyl ketone, di-sec-butyl ketone, di-tert-butyl ketone,benzophenone, methyl ethyl ketone, acetophenone, benzyl phenyl ketone,propiophenone, cyclopentanone, cyclohexanone, diacetyl, acetyl acetone,and benzoyl acetone.

Examples of the sulfoxide compound include, but are not limited to,dimethyl sulfoxide, diethyl sulfoxide, tetramethylene sulfoxide,pentamethylene sulfoxide, diphenyl sulfoxide, dibenzyl sulfoxide, andp-tolyl sulfoxide.

Examples of the carboxylic acid compound include, but are not limitedto, monobasic acids such as formic acid, acetic acid, propionic acid,butyric acid, caproic acid, lauric acid, palmitic acid, stearic acid,cyclohexylpropionic acid, cyclohexylcaproic acid, benzoic acid,phenylacetic acid, o-toluic acid, m-toluic acid, p-toluic acid, acrylicacid and methacrylic acid; dibasic acids such as oxalic acid, maleicacid, malonic acid, fumaric acid, succinic acid, adipic acid, pimelicacid, suberic acid, sebacic acid, itaconic acid, phthalic acid,isophthalic acid, terephthalic acid, naphthalic acid and diphenic acid;polybasic acid such as trimellitic acid, pyromellitic acid; and thederivatives thereof. Moreover, for example, a compound having anotherfunctional group in a single molecule thereof, such as hydroxybenzoicacid, may also be used.

Examples of the carboxylate include, but are not limited to, estersformed from monobasic acids such as formic acid, acetic acid, propionicacid, butyric acid, caproic acid, lauric acid, palmitic acid, stearicacid, cyclohexylpropionic acid, cyclohexylcaproic acid, benzoic acid,phenylacetic acid, o-toluic acid, m-toluic acid, p-toluic acid, acrylicacid and methacrylic acid, or dibasic acids such as oxalic acid, maleicacid, malonic acid, fumaric acid, succinic acid, adipic acid, pimelicacid, suberic acid, sebacic acid, itaconic acid, phthalic acid,isophthalic acid, terephthalic acid, naphthalic acid and diphenic acid,with alcohols such as methyl alcohol, ethyl alcohol, propyl alcohol,n-butyl alcohol, sec-butyl alcohol, isobutyl alcohol, tert-butylalcohol, n-amyl alcohol, iso-amyl alcohol, hexyl alcohol and an isomerthereof, heptyl alcohol and an isomer thereof, octyl alcohol and anisomer thereof, capryl alcohol, nonyl alcohol and an isomer thereof,decyl alcohol and an isomer thereof, benzyl alcohol, phenol, cresol andglycidyl alcohol; and β-ketoesters such as methyl acetoacetate and ethylacetoacetate.

Examples of the lactone compound include, but are not limited to,β-propiolactone, δ-valerolactone, ε-caprolactone, and lactone compoundscorresponding to the following acids.

Namely, examples of the acid include 2-methyl-3-hydroxypropionic acid,3-hydroxynonane or 3-hydroxypelargonic acid,2-dodecyl-3-hydroxypropionic acid, 2-cyclopentyl-3-hydroxypropionicacid, 2-n-butyl-3-cyclohexyl-3-hydroxypropionic acid,2-phenyl-3-hydroxytridecanoic acid,2-(2-ethylcyclopentyl)-3-hydroxypropionic acid, 2-methylphenyl-3-hydroxypropionic acid, 3-benzyl-3-hydroxypropionic acid,2,2-dimethyl-3-hydroxypropionic acid, 2-methyl-5-hydroxyvaleric acid,3-cyclohexyl-5-hydroxyvaleric acid, 4-phenyl-5-hydroxyvaleric acid,2-heptyl-4-cyclopentyl-5-hydroxyvaleric acid, 3-(2-cyclohexylethyl)-5-hydroxyvaleric acid, 2-(2-phenyl ethyl)-4-(4-cyclohexylbenzyl)-5-hydroxyvaleric acid, benzyl-5-hydroxyvaleric acid,3-ethyl-5-isopropyl-6-hydroxycaproic acid,2-cyclopentyl-4-hexyl-6-hydroxycaproic acid,2-cyclopentyl-4-hexyl-6-hydroxycaproic acid, 3-phenyl-6-hydroxycaproicacid, 3-(3,5-diethyl-cyclohexyl)-5-ethyl-6-hydroxycaproic acid,4-(3-phenyl-propyl)-6-hydroxycaproic acid,2-benzyl-5-isobutyl-6-hydroxycaproic acid, 7-phenyl-6-hydroxyl-octoenoicacid, 2,2-di(1-cyclohexenyl)-5-hydroxy-5-heptenoic acid,2,2-dipropenyl-5-hydroxy-5-heptenoic acid,2,2-dimethyl-4-propenyl-3-hydroxy-3,5-heptadienoic acid.

Examples of the amine compound include, but are not limited to,methylamine, ethylamine, isopropylamine, n-butylamine, sec-butylamine,tert-butylamine, n-amylamine, sec-amylamine, tert-amylamine,n-hexylamine, n-heptylamine, aniline, benzylamine, o-anisidine,m-anisidine, p-anisidine, α-naphthylamine, dimethylamine, diethylamine,di-n-propylamine, diisopropylamine, di-n-butylamine, di-sec-butylamine,diisobutylamine, di-tert-butylamine, di-n-amylamine, diisoamylamine,dibenzylamine, N-methylamine, N-ethylamine, N-ethyl-o-toluidine,N-ethyl-m-toluidine, N-ethyl-p-toluidine, triethylamine,tri-n-propylamine, tri-n-butylamine, tri-n-amylamine, triisoamylamine,tri-n-hexylamine, tribenzylamine, triphenyl methylamine, N,N-dimethylbenzylamine, N,N-dimethylamine, N,N-diethylamine,N,N-diethyl-o-toluidine, N,N-diethyl-m-toluidine,N,N-diethyl-p-toluidine, N,N-dimethyl-α-naphthylamine,N,N,N′,N′-tetramethyl ethylene diamine, N,N,N′,N′-tetraethyl ethylenediamine, pyrrolidine, piperidine, N-methylpyrrolidine,N-methylpiperidine, pyridine, piperazine, 2-acetylpyridine,N-benzylpiperazine, quinoline, morpholine.

The above-described amide compound is a compound having at least one—C(═O)—N< or —C(═S)—N< bond in a molecule thereof. Examples of the amidecompound include, but are not limited to, N,N-dimethylformamide,N-dimethylacetamide, N-methylpyrrolidone, acetamide, propionamide,benzamide, acetanilide, benzanilide, N-methylacetanilide,N,N-dimethylthioformamide, N,N-dimethyl-N,N′-(p-dimethylamino)benzamide,N-ethylene-N-methyl-8-quiniline carboxyamide, N,N-dimethyl nicotinamide,N,N-dimethyl metaacrylamide, N-methylphthalimide, N-phenylphthalimide,N-acetyl-ε-caprolactam, N,N,N′,N′-tetramethylphthalamide,10-acetylphenoxazine, 3,7-bis(dimethylamino)-10-benzoylphenothiazine,10-acetylphenothiazine, 3,7-bis)dimethylamino)-10-benzoylphenothiazine,N-ethyl-N-methyl-8-quinoline carboxyamide, and also, linear ureacompounds such as N,N′-dimethylurea, N,N′-diethylurea,N,N′-dimethylethyleneurea, N,N,N′,N′-tetramethylurea,N,N-dimethyl-N′,N′-diethylurea and N,N-dimethyl-N′,N′-diphenylurea.

Examples of the nitrile compound include, but are not limited to,1,3-butadiene monoxide, 1,3-butadiene oxide, 1,2-butylene oxide,2,3-butylene oxide, cyclohexene oxide, 1,2-epoxycyclododecane,1,2-epoxydecane, 1,2-epoxyeicosane, 1,2-epoxyheptane,1,2-epoxyhexadecane, 1,2-epoxyhexadecane, 1,2-epoxyoctadecane,1,2-epoxyoctane, ethylene glycol diglycidyl ether, 1,2-epoxytetradecane,hexamethylene oxide, isobutylene oxide, 1,7-octadiene epoxide, 2-phenylpropylene oxide, propylene oxide, trans-stilbene oxide, styrene oxide,epoxylated 1,2-polybutadiene, epoxylated inseed oil, glycidyl methylether, glycidyl n-butyl ether, glycidyl allyl ether, glycidylmethacrylate, glycidyl acrylate.

Examples of the oxime compound include, but are not limited to,acetoxime, methyl ethyl ketone oxime, diethyl ketone oxime, acetophenoneoxime, benzophenone oxime, benzyl phenyl ketone oxime, cyclopentanoneoxime, cyclohexanone oxime, and benzaldehyde oxime.

The above described component (D) that is a polar compound may be usedalone as one kind or in combinations of two kinds or more.

As such a polar compound, a polar compound having no active hydrogen ispreferable. Among others, an amine compound and an ether compound aremore preferable, and an amine compound is further preferable.

From the perspective of high activity of hydrogenation of a catalystcomposition for hydrogenation produced by the production method of thepresent embodiment at the initial stage of production and after storagethereof, and a low degree of filter clogging in an extruder upon theproduction of a hydrogenated unsaturated double bond-containingcompound, the mass ratio of component (D) and component (A) ((D)/(A)) ispreferably 0.01 or more. On the other hand, from the perspective ofstorage stability or economical efficiency, the mass ratio ((D)/(A)) ispreferably 2 or less.

The mass ratio of component (D) and component (A) ((D)/(A)) is morepreferably in a range of 0.01 to 1, even more preferably in a range of0.015 to 0.50, further preferably in a range of 0.020 to 0.30, and stillfurther preferably in a range of 0.015 to 0.30.

(Mixing Method)

In the method for producing a catalyst composition for hydrogenation ofthe present embodiment, the above described component (A), component (B)and component (C), and optionally component (D), and optionally using apredetermined solvent are mixed.

From the perspective of high activity of hydrogenation and a low degreeof filter clogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound, in the method for producinga catalyst composition for hydrogenation of the present embodiment, ashearing force is applied at a shearing rate of 1000 (1/s) or more to atleast component (A). This step is referred to as a “force applicationstep” in the present specification.

<Force Application Step>

In the above-described force application step, example of an apparatusfor applying a shearing force include, but are not limited to, astirrer, a homogenizer including emulsification equipment, and a pump.

From the perspective of high activity of hydrogenation or a low degreeof filter clogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound, the shearing rate is set at1000 (1/s) or more, and it is preferably 3,000 (1/s) or more, and morepreferably 10,000 (1/s) or more.

The term “shearing rate” used herein means a shearing rate at a site atwhich the shearing rate of the above described apparatus used to apply ashearing force becomes the maximum.

For instance, the shearing rate (Vs) of a device comprising a rotor(rotation portion) that rotates at a constant rate and a stator (fixedportion) is obtained by dividing the peripheral velocity (Vu) of therotor by a minimum gap (d) between the rotor and the stator (Vs(1/s)=Vu/d).

In general, the peripheral velocity of a rotor increases as themeasurement point of the velocity approaches to the outer side of therotor. Therefore, if gap (d) is constant independent of the place in thedevice, a value obtained by dividing the peripheral velocity of theoutermost side of the rotor by gap (d) is defined as a shearing rate inthe present embodiment.

In terms of high activity of hydrogenation and a low degree of filterclogging in an extruder upon the production of a hydrogenatedunsaturated double bond-containing compound, the time required forapplication of such a shearing force is preferably 5 minutes or more andwithin 72 hours, more preferably 20 minutes or more and within 48 hours,and further preferably within 2 to 24 hours.

If component (A) is a solid, it is preferable to finely crush the solidby applying a shearing force thereto.

From the perspective of high activity of hydrogenation of a catalystcomposition for hydrogenation at the initial stage of production andafter storage thereof, and a low degree of filter clogging in anextruder upon the production of a hydrogenated unsaturated doublebond-containing compound, it is preferable to mix component (A) withcomponent (B) after a shearing force has been applied to component (A).

When component (B) is added to component (A) that is a solid, the meanparticle diameter of the component (A) is preferably 100 μm or less,from the perspective of activity of hydrogenation and filter clogging inan extruder. The mean particle diameter of component (A) is morepreferably 50 μm or less, even more preferably 30 μm or less, andfurther preferably 15 μm or less.

The state of component (A) upon application of a shearing force is notparticularly limited. It may be any one of a liquid state, asolid-liquid mixed state, and a solid state. From the perspective ofhandling, the state of component (A) is preferably a liquid state or asolid-liquid mixed state.

From the perspective of high activity of hydrogenation of a catalystcomposition for hydrogenation at the initial stage of production andafter storage thereof, and a low degree of filter clogging in anextruder upon the production of a hydrogenated unsaturated doublebond-containing compound, the method for producing a catalystcomposition for hydrogenation of the present embodiment more preferablycomprises a step of mixing after adding component (B) to a mixture ofcomponent (A) and component (C).

From the perspective of high activity of hydrogenation of a catalystcomposition for hydrogenation both at the initial stage of productionand after storage thereof, and a low degree of filter clogging in anextruder upon the finishing of a hydrogenated unsaturated doublebond-containing compound, the method for producing a catalystcomposition for hydrogenation of the present embodiment more preferablycomprises a step of mixing component (A), component (B), component (C),and component (D) after adding component (B) to a mixture of component(A) and component (C), after or during the force application step.

From the perspective of high activity of hydrogenation of a catalystcomposition for hydrogenation both at the initial stage of productionand after storage thereof, and a low degree of filter clogging in anextruder upon the production of a hydrogenated unsaturated doublebond-containing compound, the method for producing a catalystcomposition for hydrogenation of the present embodiment furtherpreferably comprises a step of mixing component (A), component (B),component (C), and component (D) after adding component (B) to a mixtureof component (A), component (C) and component (D), after or during theforce application step.

The catalyst composition for hydrogenation has been previously preparedin a catalyst tank that is different from a reaction system containing atarget to be hydrogenated, and it may be then introduced into thereaction system in which the target to be hydrogenated is present, asdescribed later. Alternatively, individual ingredients of the catalystcomposition for hydrogenation may be introduced into reaction system,separately.

Since the catalyst composition for hydrogenation obtained by theproduction method of the present embodiment is excellent in storagestability, it is suitably used in a method of preparing the catalystcomposition for hydrogenation in a different catalyst tank and thenintroducing it into a reaction system.

In a case in which the target to be hydrogenated is a conjugated dienepolymer or a copolymer formed of a conjugated diene and a vinyl aromatichydrocarbon, wherein the polymer or the copolymer has been produced byliving anionic polymerization using an organic alkaline metal or anorganic alkaline-earth metal as an initiator, the active end of thepolymer or copolymer can also be partially or entirely utilized as abovedescribed component (B) when the ingredients of a catalyst compositionfor hydrogenation are introduced into a reaction system for thehydrogenation step.

Moreover, before hydrogenation and after the polymerization of a polymeror a copolymer as a target to be hydrogenated, the active end may bepartially or entirely deactivated.

When the ingredients of the catalyst composition for hydrogenation areeach separately introduced into a reaction system, if an excessdeactivator for the active end of a polymer or copolymer as a target tobe hydrogenated is present in the reaction system, such a deactivatormay also be considered to be component (D) or a part of component (D).

In such a case, the above-described mass ratio of component (D) tocomponent (A) ((D)/(A)) is calculated, estimating such an excessdeactivator as component (D).

When a catalyst composition for hydrogenation is produced in advance ina catalyst tank that is different from a reaction system in which atarget to be hydrogenated is present, the atmosphere may be an inertatmosphere or a hydrogen atmosphere.

The temperature applied to the production and storage of the catalystcomposition for hydrogenation is preferably in a range of −50° C. to 50°C., and more preferably −20° C. to 30° C.

The time required for the production of the catalyst composition forhydrogenation is different depending on the production temperature.Under conditions of a production temperature of 25° C., it is severalminutes to 60 days, and preferably 1 minute to 20 days.

When the catalyst composition for hydrogenation is produced in advancein a catalyst tank that is different from a reaction system in which atarget to be hydrogenated is present, if component (A), component (B),component (C) and component (D) that constitute the catalyst compositionfor hydrogenation are used in the form of a solution prepared bydissolving these components in an inactive organic solvent, it is easilyhandled, and thus it is preferable.

The inactive organic solvent used in the case in which the componentsare used in the form of a solution is preferably a solvent that does notreact with any forms associated with the hydrogenation reaction. It ispreferably the same solvent as that used in the hydrogenation reaction.

When the catalyst composition for hydrogenation is produced in advancein a catalyst tank that is different from a reaction system in which atarget to be hydrogenated is present, the produced catalyst compositionfor hydrogenation is transferred to a hydrogenation reactor(hydrogenation tank) in which the target to be hydrogenated iscontained. From the perspective of the achievement of high activity ofhydrogenation, this operation is preferably carried out under a hydrogenatmosphere.

From the perspective of high activity of hydrogenation and suppressionof the yellowing of a hydrogenated polymer, the temperature applied tothe transfer of the catalyst composition for hydrogenation is preferablya temperature of −30° C. to 100° C., and more preferably −10° C. to 50°C.

Also, from the perspective of high activity of hydrogenation, thecatalyst composition for hydrogenation is preferably added to the targetto be hydrogenated, immediately before initiation of the hydrogenationreaction.

With regard to the mixing ratio of individual components necessary forexhibiting high activity of hydrogenation and hydrogenation selectivity,the ratio of the metal mole number of component (B) to the metal (Ti)mole number of component (A) (hereinafter referred to as a “molar ratioof Metal (B)/Metal (A)) is preferably in a range of approximately 20 orless.

By determining the mixing ratio of component (A) to component (B) suchthat the molar ratio of Metal (B)/Metal (A) is in a range of 0.5 to 10,the activity of hydrogenation of the catalyst composition forhydrogenation can be improved. Thus, the above-described molar ratio ismost preferable.

When the target to be hydrogenated is a living polymer obtained byliving anionic polymerization, the living end acts as a reductant. Thus,when a polymer having a living active end is hydrogenated, from theperspective of achieving the above-described optimal molar ratio ofMetal (B)/Metal (A), and carrying out a stable hydrogenation reactionfor a longer period of time, the living active end is more preferablydeactivated with various compounds having active hydrogen or halogen.

Examples of the above described compound having active hydrogen include,but are not limited to, water, alcohols such as methanol, ethanol,n-propanol, n-butanol, sec-butanol, t-butanol, 1-pentanol, 2-pentanol,3-pentanol, 1-hexanol, 2-hexanol, 3-hexanol, 1-heptanol, 2-heptanol,3-heptanol, 4-heptanol, octanol, nonanol, decanol, undecanol, laurylalcohol, allyl alcohol, cyclohexanol, cyclopentanol and benzyl alcohol,and phenols such as phenol, o-cresol, m-cresol, p-cresol, p-allylphenol,2,6-di-t-butyl-p-cresol, xylenol, dihydroanthraquinone,dihydroxycoumarin, 1-hydroxyanthraquinone, m-hydroxybenzyl alcohol,resorcinol and leucoaurin.

Moreover, examples of the acid include, but are not limited to, organiccarboxylic acids such as acetic acid, propionic acid, butyric acid,isoacetic acid, pentanoic acid, hexanoic acid, heptanoic acid, decalinacid, myristic acid, stearic acid, behenic acid, and benzoic acid.

Furthermore, examples of the compound having halogen include, but arenot limited to, benzyl chloride, trimethylsilyl chloride (bromide),t-butylsilyl chloride (bromide), methyl chloride (bromide), ethylchloride (bromide), propyl chloride (bromide), and n-butyl chloride(bromide).

These acids may be used alone as one kind or in combination of two kindsor more.

[Catalyst Composition For Hydrogenation]

As described above, a catalyst composition for hydrogenation can beobtained by using a titanocene compound (A), a compound (B) containingat least one element selected from the group consisting of elements Li,Na, K, Mg, Zn, Al and Ca, and an unsaturated compound (C), applying ashearing force at a shearing rate of 1000 (1/s) or more to at least thecomponent (A), and mixing the (A), (B) and (C).

[Hydrogenation Method Using Catalyst Composition for Hydrogenation]

The catalyst composition for hydrogenation produced by the productionmethod of the present embodiment can be used in a step of hydrogenatingproducts to be hydrogenated, which are all compounds having an olefinicunsaturated double bond.

The catalyst composition for hydrogenation can be applied, for example,to low molecular weight polymers containing at least one olefinicunsaturated double bond in a molecule thereof, including: aliphaticolefins such as ethylene, propylene, butene, pentene, hexene, heptene,octene, or an isomer thereof; alicyclic olefins such as cyclopentene,methylcyclopentene, cyclopentadiene, cyclohexene, methylcyclohexene, orcyclohexadiene; monomers such as styrene, butadiene, or isoprene; andunsaturated fatty acids and derivatives thereof, and an unsaturatedliquid oligomers.

In addition, the catalyst composition for hydrogenation produced by theproduction method of the present embodiment can also be applied to theselective hydrogenation of an olefinic unsaturated double bond in aconjugated diene polymer or in a copolymer formed of a conjugated dieneand an olefin monomer.

The term “selective hydrogenation” used herein means that an olefinicunsaturated double bond in a conjugated diene portion of a conjugateddiene polymer or of a copolymer formed of a conjugated diene and anolefin monomer is selectively hydrogenated. For instance, it means thata carbon-carbon double bond in the aromatic ring is not substantiallyhydrogenated when a vinyl aromatic compound is used as such an olefinmonomer.

A selectively hydrogenated product of the olefinic unsaturated doublebond of a conjugated diene polymer or of a copolymer formed of aconjugated diene and an olefin monomer is industrially useful as anelastic body or a thermoplastic elastic body.

If the above described product to be hydrogenated is a conjugated dienepolymer or a copolymer formed of conjugated diene, the conjugated dienemay generally be a conjugated diene having 4 to about 12 carbon atoms.Examples of the conjugated diene include, but are not limited to,1,3-butadiene, isoprene, 2,3-dimethyl-1,3-butadiene, 1,3-pentadiene,2-methyl-1,3-pentadiene, 1,3-hexadiene, 4,5-diethyl-1,3-octadiene, and3-butyl-1,3-octadiene.

From the perspective of obtaining an elastic body that is industriallyadvantageously developed and is excellent in physical properties, amongthese conjugated dienes, 1,3-butadiene and isoprene are preferable.

The microstructure of the butadiene portion includes a 1,2-bond and a1,4-bond (cis+trans). The catalyst composition for hydrogenation of thepresent embodiment can quantitatively hydrogenate both of them.

In addition, in the isoprene portion, olefinic unsaturated bonds arefound in the side chains of a 1,2-bond and a 3,4-bond and in the mainchain of a 1,4-bond (cis+trans). The catalyst composition forhydrogenation obtained by the production method of the presentembodiment can quantitatively hydrogenate all of them.

The structure and rate of hydrogenating a compound with the catalystcomposition for hydrogenation of the present embodiment can beidentified using 1H-NMR.

According to the hydrogenation method using the catalyst composition forhydrogenation produced by the production method of the presentembodiment, the 1,2-bond and 1,4-bond in the butadiene portion and theside chains of the 1,2-bond and 3,4-bond of the isoprene portion can beparticularly selectively hydrogenated.

When 1,3-butadiene is selected as a main ingredient of a conjugateddiene polymer hydrogenated with the catalyst composition forhydrogenation, the amount of a 1,2-bond as a microstructure of abutadiene unit portion in a target to be hydrogenated is preferably 8%or more, more preferably 20% or more, and further preferably 30% to 80%,in order to allow the elasticity of an elastomer to exhibit, inparticular, at a temperature ranging from a low temperature to roomtemperature.

Moreover, when isoprene is selected as a main ingredient of a conjugateddiene polymer in a target to be hydrogenated, which is hydrogenated withthe catalyst composition for hydrogenation, the amount of a 1,4-bond asa microstructure of an isoprene unit portion in the target to behydrogenated is preferably 50% or more, and more preferably 75% or more,for the same reason as that described above.

In order to allow the catalyst composition for hydrogenation tosufficiently exhibit the effect of selectively hydrogenating only theunsaturated double bond in a conjugated diene unit of a target to behydrogenated, and in order to obtain an elastic body or a thermoplasticelastic body that is industrially useful and highly valuable, it ispreferable to use a copolymer formed of a conjugated diene and avinyl-substituted aromatic hydrocarbon as a target to be hydrogenated.

Examples of a vinyl aromatic hydrocarbon that is copolymerizable with aconjugated diene include, but are not limited to, styrene,tert-butylstyrene, α-methylstyrene, p-methylstyrene, divinylbenzene,1,1-diphenylethylene, N,N-dimethyl-p-aminoethylstyrene, andN,N-diethyl-p-aminoethylstyrene. In particular, from the perspective ofthe ease of polymerization and economical efficiency, styrene anda-methylstyrene are preferable.

Preferred examples of the above described copolymer formed of aconjugated diene and a vinyl-substituted aromatic hydrocarbon include,but are not limited to, a butadiene/styrene copolymer, anisoprene/styrene copolymer, and a butadiene/isoprene/styrene copolymer,since industrially valuable hydrogenated copolymers can be obtained fromthese copolymers. Such a copolymer of a conjugated diene and avinyl-substituted aromatic hydrocarbon may be any one of a randomcopolymer, a block copolymer, a tapered block copolymer and the like,and thus, the type of the copolymer is not particularly limited.

When the catalyst composition for hydrogenation produced by theproduction method of the present embodiment is used under preferredhydrogenation conditions described later, hydrogenation of acarbon-carbon double bond (aromatic ring) of a vinyl-substitutedaromatic hydrocarbon unit in such a copolymer does not substantiallytake place.

The hydrogenation reaction, in which the catalyst composition forhydrogenation produced by the production method of the presentembodiment is used, is preferably carried out by allowing a target to behydrogenated to come into contact with hydrogen in a solution preparedby dissolving a target to be hydrogenated in an inactive organicsolvent.

The term “inactive organic solvent” used herein means a solvent thatdoes not react with any forms associated with the hydrogenationreaction.

Examples of such an inactive organic solvent include, but are notlimited to, aliphatic hydrocarbons such as n-pentane, n-hexane,n-heptane, and n-octane; alicyclic hydrocarbons such as cyclohexane,cycloheptane, and cycloheptane; and ethers such as diethyl ether andtetrahydrofuran. These solvents may be used singly as only one type orin the form of a mixture of two or more types of solvents.

Moreover, aromatic hydrocarbons such as benzene, toluene, xylene, andethyl benzene may also be used, only in a case in which an aromaticdouble bond is not hydrogenated under the selected hydrogenationconditions.

The hydrogenation reaction is generally carried out by retaining theabove-described solution containing a target to be hydrogenated at apredetermined temperature under a hydrogen or inert atmosphere, adding acatalyst composition for hydrogenation to the solution while stirring ornot stirring, and then introducing hydrogen gas to compress it to apredetermined pressure. The term “inert atmosphere” used herein means anatmosphere that does not react with any forms associated with thehydrogenation reaction, such as nitrogen, helium, neon or argon. The airatmosphere or oxygen atmosphere is not preferable because it oxidizes acatalyst composition for hydrogenation, thereby causing deactivation ofthe catalyst composition for hydrogenation.

Since the catalyst composition for hydrogenation produced by theproduction method of the present embodiment is excellent in storagestability, it is preferably used in a hydrogenation method involvingcontinuously supplying a target to be hydrogenated and a catalystcomposition for hydrogenation to a reactor in which a hydrogenationreaction is carried out (continuous hydrogenation).

Moreover, the catalyst composition for hydrogenation produced by theproduction method of the present embodiment can also be used in abatch-type hydrogenation method.

The amount of the catalyst composition for hydrogenation added in thehydrogenation step is preferably 0.001 to 20 mmol per 100 g of a targetto be hydrogenated, in terms of the molar amount of component (A).

If the amount of the catalyst composition for hydrogenation added is setin this additive amount range, it is possible to preferentiallyhydrogenate an olefinic unsaturated double bond, when the target to behydrogenated is a copolymer formed of a conjugated diene and avinyl-substituted aromatic hydrocarbon. Thus, hydrogenation of thedouble bond of an aromatic ring in the copolymer does not substantiallytake place. Hence, extremely high hydrogenation selectivity can berealized.

Even if the amount of the catalyst composition for hydrogenation addedis more than 20 mmol per 100 g of a target to be hydrogenated, in termsof the molar amount of component (A), the hydrogenation reaction can becarried out. However, the use of an unnecessary amount of catalystcomposition for hydrogenation is economically inefficient, and further,since it needs complicated operations such as the removal of thecatalyst composition for hydrogenation and decalcification after thehydrogenation reaction, it is disadvantageous for the step.

The amount of the catalyst composition for hydrogenation used toquantitatively hydrogenate the unsaturated double bond of a conjugateddiene unit of a polymer under the selected conditions can be preferably0.01 to 5 mmol per 100 g of a target to be hydrogenated, in terms of themolar amount of component (A).

In the hydrogenation reaction, gaseous hydrogen is preferably introducedinto a hydrogenation reaction tank.

The hydrogenation reaction is more preferably carried out understirring, and thereby, the introduced hydrogen is allowed tosufficiently quickly come into contact with the target to behydrogenated.

The hydrogenation reaction is generally carried out in a temperaturerange of 0° C. to 200° C.

If the temperature is lower than 0° C., the hydrogenation speed becomesslow, and thus, since a large amount of catalyst composition forhydrogenation is required, it is not economically efficient. On theother hand, if the temperature is higher than 200° C., side reactions,decomposition and gelatinization easily occur in combination with thehydrogenation reaction, and also, the catalyst composition forhydrogenation is likely to be deactivated. As a result, the activity ofhydrogenation unfavorably decreases.

A more preferred temperature range is 20° C. to 180° C.

The hydrogen pressure used in the hydrogenation reaction is preferably 1to 100 kgf/cm².

If the hydrogen pressure is less than 1 kgf/cm², the hydrogenation speedbecomes slow, and thus, the hydrogenation rate becomes insufficient. Ifthe hydrogen pressure is more than 100 kgf/cm², the hydrogenationreaction is almost completed at the same time as pressure rising, and itunfavorably results in unnecessary side reactions or gelatinization.

A more preferred hydrogen pressure applied to hydrogenation is 2 to 30kgf/cm², and an optimal hydrogen pressure is selected based on thecorrelation with the amount of the catalyst composition forhydrogenation added, etc. Substantially, it is preferable that a higherhydrogen pressure be selected to carry out the hydrogenation reaction,as the above-described amount of the catalyst composition forhydrogenation decreases.

In addition, the time required for the hydrogenation reaction isgenerally several seconds to 50 hours.

The hydrogenation reaction time and the hydrogenation pressure areappropriately selected in the above-described ranges, depending on adesired hydrogenation rate.

By the above-described hydrogenation step, any desired hydrogenationrate depending on purposes can be obtained from the olefinic unsaturateddouble bond of an olefin compound, and from the olefinic unsaturateddouble bonds of a conjugated diene copolymer and a copolymer formed of aconjugated diene and a vinyl aromatic hydrocarbon.

After the hydrogenation reaction has been carried out using the catalystcomposition for hydrogenation produced by the production method of thepresent embodiment, a hydrogenated product can be easily separated froma solution containing the hydrogenated product by chemical or physicalmeans such as distillation or precipitation.

In particular, when the target to be hydrogenated is a polymer, aresidue of catalyst composition for hydrogenation can be removed fromthe polymer solution obtained after the hydrogenation reaction, asnecessary, and the hydrogenated polymer can be then separated from thesolution.

Examples of the separation method include a method comprising adding apolar solvent serving as a poor solvent to the hydrogenated polymer,such as acetone or alcohol, to the reaction solution after thehydrogenation to precipitate the hydrogenated polymer and thenrecovering it, a method comprising adding the reaction solution afterthe hydrogenation to boiling water while stirring, and then distillingto recover the hydrogenated polymer together with the solvent, and amethod comprising directly heating the reaction solution to distill awaythe solvent.

EXAMPLES

Hereinafter, the present invention will be described in detail by way ofthe following specific examples and comparative examples. However, theseexamples are not intended to limit the scope of the present invention.

First, evaluation methods carried out in the examples and thecomparative examples will be described below.

[Evaluation Method] <Hydrogenation Rate>

Batch-type hydrogenation was carried out in Examples 1 to 18, Examples21 to 34, Comparative Examples 1 to 8, and Comparative Examples 11 to13, whereas continuous hydrogenation was carried out in Examples 19, 20,35 and 36, and Comparative Examples 9, 10, 14 and 15.

In all of the examples and the comparative examples, a catalystcomposition for hydrogenation was added, such that the amount of Tibecame 150 ppm based on the after-described polymer solution to behydrogenated, and thereafter, a hydrogenation reaction was carried outat a hydrogen pressure of 5 kgf/cm² at a temperature of 90° C. and aretention time of 30 minutes. The hydrogenation rate obtained wasmeasured using NMR as described later.

After the production of a catalyst composition for hydrogenation, both acase in which it was used immediately after the production (initialstage) and a case in which it was used after it had been stored at 30°C. for 30 days were evaluated.

It was considered that a higher hydrogenation rate was better, and thehydrogenation rate that was 99.5% or more was evaluated as ⊚,

the hydrogenation rate that was 99.0% or more and less than 99.5% wasevaluated as ◯,the hydrogenation rate that was 97.0% or more and less than 99.0% wasevaluated as Δ, andthe hydrogenation rate that was less than 97% was evaluated as x.

(NMR: Method of Measuring Hydrogenation Rate)

The hydrogenation rate of unsaturated groups in a conjugated diene wasmeasured using nuclear magnetic resonance spectrum analysis (NMR) underthe following conditions.

After the hydrogenation reaction, the reaction product was precipitatedin a large amount of methanol to recover a hydrogenated polymer, andthereafter, the hydrogenated polymer was subjected to extraction withacetone and vacuum drying, and 1H-NMR measurement was then carried out.

Measurement apparatus: JNM-LA400 (manufactured by JEOL)

Solvent: deuterated chloroform

Measurement sample: samples obtained before and after hydrogenation ofthe after-described polymer to be hydrogenated

Sample concentration: 50 mg/mL

Measuring frequency: 400 MHz

Chemical shift standard: TMS (tetramethylsilane)

Pulse delay: 2.904 seconds

Number of scannings: 64

Pulse width: 45°

Measurement temperature: 26° C.

<Filter Clogging in Extruder>

0.3 Parts by mass ofoctadecyl-3-(3,5-di-t-butyl-4-hydroxyphenyl)propionate was added as astabilizer to 100 parts by mass of a hydrogenated polymer that had beensubjected to a hydrogenation reaction with a catalyst composition forhydrogenation immediately after the production thereof (initial stage),which had been used in the above described measurement of ahydrogenation rate.

An α-(p-nonylphenyl)-ω-hydroxypoly(oxyethylene) mixture of dihydrodienephosphate and monohydrodiene phosphate (wherein the oxyethylene unit ofpoly(oxyethylene) was 9 to 10 as a mean value) was added as a crumbingagent to water for stripping, resulting in a concentration of 20 ppm.Thereafter, stripping was carried out at a temperature of 90° C. to 98°C., and the solvent was then removed.

After the removal of the solvent from the tank, the concentration of thepolymer in slurry after the above-described stripping in the tank wasapproximately 5% by mass.

Subsequently, the slurry that was a water dispersion of the aboveobtained crumb-like polymer was supplied to a rotation screen, andhydrated crumb with a water content of approximately 45% by mass wasobtained. This hydrated crumb was supplied to a single screwextruder-type water wringing device to obtain a dehydrated polymer.

Thereafter, the above obtained polymer (hydrogenated polymer) wassupplied to a twin screw one vented extruder, and it was extruded at acylinder temperature of 220° C., at a screw rotation number of 200 rpm,at a vent pressure of approximately 200 mmHg (absolute pressure), andwas then dried.

During this operation, as the time required until a 200-mesh filterequipped into the tip section of the extruder was clogged and thepressure became 20 kgf/cm² or more was prolonged, it was determined tobe economically favorable, and the filter clogging was then evaluatedaccording to the following standards.

The period of time that was 3 hours or more was evaluated as excellent⊚,

the period of time that was 2 hours or more and less than 3 hours wasevaluated as good ◯,

the period of time that was 1 hour or more and less than 2 hours wasevaluated as fair Δ, and

the period of time that was less than 1 hour was evaluated as poor x.

Constitutional components of a catalyst composition for hydrogenationproduced in each of the examples and the comparative examples will bedescribed below.

Component (A) (A-1): Synthesis of bis(η(5)-cyclopentadienyl)titaniumdi(p-tolyl)

200 Milliliter of anhydrous ether was added to a three-necked flaskequipped with a stirrer, a dripping funnel and a reflux condenser(hereinafter also referred to as a “device”).

The device was dried with dry helium, and 17.4 g (2.5 mol) of a piece oflithium wire was then cut and dropped into the flask. Thereafter, asolution of 300 mL of ether and 171 g (1 mol) of p-bromotoluene wasadded in a small amount dropwise to the flask at room temperature, andthe total amount of ether solution of p-bromotoluene was gradually addedthereto under reflux.

After the reaction, the reaction solution was filtrated under a heliumatmosphere, so as to obtain a colorless transparent p-tolyl lithiumsolution.

To a 2-L three-necked flask equipped with a stirrer and a drippingfunnel, which had been substituted with dry helium, 99.6 g (0.4 mol) ofbis(η(5)-cyclopentadienyl)titanium dichloride and 500 mL of anhydrousether were added.

The previously synthesized ether solution of p-tolyl lithium was addeddropwise to the above-described flask at room temperature under stirringfor approximately 2 hours.

Thereafter, the reaction mixture was separated by filtration in the air,and an insoluble portion was then washed with dichloromethane. Thefiltrate was gathered with the washing solution, and the solvent wasthen removed under reduced pressure.

The residue was dissolved in a small amount of dichloromethane, andpetroleum ether was then added to the solution to carry outrecrystallization.

The obtained crystal was separated by filtration, and the filtrate wasthen concentrated again. Thus, the above-described operations wererepeatedly carried out to obtain bis(η(5)-cyclopentadienyl)titaniumdi(p-tolyl).

The yield was 87%.

The obtained crystal had an orange-yellow needle form, and thesolubility in toluene and cyclohexane was high. The crystal had amelting point of 145° C. and element analysis value: C, 80.0; H, 6.7;Ti, 13.3.

(A-2): Synthesis of bis(η(5)-cyclopentadienyl)titanium di(phenyl)

157 Grams (1 mol) of bromobenzene was used instead of the p-bromotolueneused in above described (A-1). Other than this exception, the sameconditions as those in above described (A-1) were applied to synthesizephenyl lithium.

Using the phenyl lithium, bis(η(5)-cyclopentadienyl)titanium diphenylwas obtained by the same step as that in above described (A-1). Theyield amount was 120 g (yield: 90%). The obtained crystal had anorange-yellow needle form, and the solubility in toluene and cyclohexanewas slightly high. The crystal had a melting point of 147° C. andelement analysis value: C, 79.5; H, 6.1; Ti, 14.4.

(A-3): Synthesis of bis(η(5)-cyclopentadienyl)titanium di(3,4-xylyl)

4-Bromo-o-xylene (1 mol) was used instead of the p-bromotoluene used inabove described (A-1). Other than this exception, the same conditions asthose in above described (A-1) were applied to synthesizebis(η(5)-cyclopentadienyl)titanium di(3,4-xylyl). The yield was 83%. Theobtained crystal had a yellow needle form, and the solubility in tolueneand cyclohexane was high. The crystal had a melting point of 155° C. andelement analysis value: C, 80.6; H, 7.2; Ti, 12.2.

(A-4): Bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dichloride

A product obtained by recrystallization of a reagent manufactured byNIHON FINE CHEMICAL Co., Ltd. in dichloromethane was used.

Component (B)

(B-1): Triethyl aluminum; hexane solution (manufactured by Tosoh AkzoCorp.) was directly used.(B-2): sec-Butyl lithium; hexane solution (manufactured by KANTOCHEMICAL CO., INC.) was separated by filtration under an inertatmosphere, and a yellow transparent portion was used.

Component (C)

(C-PB): Polybutadiene (Ricon 142, manufactured by Ricon; the ratio ofthe olefinic unsaturated double bond content of side chains based on thetotal olefinic unsaturated double bond content was 0.55, and the numberaverage molecular weight was 4000) was used.

(C-1): Myrcene (C-2): Isoprene (C-3): 1,7-Octadiene Component (D) (D-1):Tetrahydrofuran

(D-2): N,N,N′,N′-tetramethylethylenediamine

Examples 1 to 20 and [Comparative Examples 1 to 10]

A catalyst composition for hydrogenation was produced as follows.

In Examples 1 to 15, Examples 18 to 20, and Comparative Examples 1 to10, component (A), component (C), and component (D) were mixed at theratio shown in Table 1 below. Thereafter, using the below-describeddevice, a shearing force was applied to the obtained mixture for 2 hoursunder the below-described conditions, and component (B) was then addedto the reaction mixture, followed by application of a shearing force for30 minutes.

In Example 16, component (A) was mixed with component (C) at the ratioshown in Table 1 below. Thereafter, using the below-described device, ashearing force was applied to the obtained mixture for 2 hours under thebelow-described conditions, and component (B) was then added to thereaction mixture, followed by application of a shearing force for 30minutes. Thereafter, component (D) was added to the reaction mixture,and a shearing force was applied thereto for 30 minutes.

In Example 17, the ratio shown in Table 1 below was applied, and ashearing force was applied to component (A) for 2 hours using thebelow-described device under the below-described conditions. Thereafter,component (B) was added to the reaction mixture, and a shearing forcewas then applied thereto for 30 minutes. Thereafter, component (C) andcomponent (D) were added to the reaction mixture, and a shearing forcewas then applied thereto for 30 minutes.

(Device and Conditions for Applying Shearing Force, Used in Examples 1to 4, 7, and 9 to 20)

Homogenizer: Homo Mixer MARKII (PRIMIX, trade name, 0.2 kW)

Throughput: 1.5 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 1200 rpm, Shearing rate: 3500 (1/s)

(Device and Conditions for Applying Shearing Force, Used in Example 5)

Homogenizer: Homo Mixer MARKII (PRIMIX, trade name, 0.2 kW)

Throughput: 1.5 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 12000 rpm, Shearing rate: 35000 (1/s)

(Device and Conditions for Applying Shearing Force, Used in Examples 6and 8)

Emulsifying disperser: CAVITRON CD1010 (Pacific Machinery & EngineeringCo., Ltd., trade name, 7.5 kW)

Throughput: 100 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 5000 rpm, Shearing rate: 51600 (1/s)

(Device and Conditions for Applying Shearing Force, Used in ComparativeExamples 1 to 10)

Emulsifying disperser: Homo Disper (PRIMIX, trade name, 0.2 kW)

Throughput: 2.5 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 600 rpm, Shearing rate: 126 (1/s)

Examples 21 to 36 and [Comparative Examples 11 to 15]

A catalyst composition for hydrogenation was produced as follows.

In Examples 21 to 28, Examples 31 to 36, and Comparative Examples 11 to15, component (A), component (C), and component (D) were mixed at theratio shown in Table 2 below. Thereafter, using the below-describeddevice, a shearing force was applied to the obtained mixture for 2 hoursunder the below-described conditions, and component (B) was then addedto the reaction mixture, followed by application of a shearing force for30 minutes.

In Example 29, component (A) was mixed with component (C) at the ratioshown in Table 2 below. Thereafter, using the below-described device, ashearing force was applied to the obtained mixture for 2 hours under thebelow-described conditions, and component (B) was then added to thereaction mixture, followed by application of a shearing force for 30minutes. Thereafter, component (D) was added to the reaction mixture,and a shearing force was applied thereto for 30 minutes.

In Example 30, the ratio shown in Table 2 below was applied, and ashearing force was applied to component (A) for 2 hours using thebelow-described device under the below-described conditions. Thereafter,component (B) was added to the reaction mixture, and a shearing forcewas then applied thereto for 30 minutes. Thereafter, component (C) andcomponent (D) were added to the reaction mixture, and a shearing forcewas then applied thereto for 30 minutes.

(Device and Conditions for Applying Shearing Force, Used in Examples 21to 23, 25, and 27 to 36)

Homogenizer: Homo Mixer MARKII (PRIMIX, trade name, 0.2 kW)

Throughput: 1.5 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 1200 rpm, Shearing rate: 3500 (1/s)

(Device and Conditions for Applying Shearing Force, Used in Example 24)

Homogenizer: Homo Mixer MARKII (PRIMIX, trade name, 0.2 kW)

Throughput: 1.5 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 12000 rpm, Shearing rate: 35000 (1/s)

(Device and Conditions for Applying Shearing Force, Used in Example 26)

Emulsifying disperser: CAVITRON CD1010 (Pacific Machinery & EngineeringCo., Ltd., trade name, 7.5 kW)

Throughput: 100 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 5000 rpm, Shearing rate: 51600 (1/s)

(Device and Conditions for Applying Shearing Force, Used in ComparativeExamples 11 to 15)

Emulsifying disperser: Homo Disper (PRIMIX, trade name, 0.2 kW)

Throughput: 2.5 kg of a cyclohexane solution containing 4% by mass ofcomponent (A)

Rotation number: 600 rpm, Shearing rate: 126 (1/s)

[Polymer to be Hydrogenated]

A polymer to be hydrogenated was produced as follows.

(Polymerization of Styrene-Butadiene-Styrene Block Copolymer)

400 Kg of cyclohexane, 15 kg of styrene monomer, 110 g of n-butyllithium, and 2.5 kg of tetrahydrofuran were added into an autoclave, andthe mixture was then polymerized under stirring at 60° C. for 3 hours.Subsequently, 70 kg of 1,3-butadiene monomer was added to the reactionmixture, and the thus obtained mixture was then polymerized at 60° C.for 3 hours.

Finally, 15 kg of styrene monomer was added to the reaction mixture, andthe thus obtained mixture was then polymerized at 60° C. for 3 hours.

The active end was deactivated with water.

The obtained styrene-butadiene-styrene copolymer was a complete blockcopolymer, and the styrene content was 30% by mass, the content of the1,2-vinyl bond of a butadiene unit was 45 mol %, and the weight averagemolecular weight measured using GPC (molecular weight in terms ofpolystyrene) was approximately 60,000.

The above described styrene content and the content of the 1,2-vinylbond of the butadiene unit were measured using NMR, which had been usedin the above described measurement of a hydrogenation rate.

The evaluation results regarding the hydrogenation rate of each polymerand filter clogging in an extruder are shown in the following Table 1and Table 2.

TABLE 1 Catalyst composition for hydrogenation (C) (D) Evaluationresults Mass Mass Shear- Rate of hydro- Filter ratio ratio ing genatingpolymer clogging (A) (B) to (A) to (A) rate Initial After in Type (mmol)Type (mmol) Type (−) Type (−) (1/s) stage 30 days extruder Example 1 A-10.015 B-1 0.0375 C-PB 4 D-2 — 3500 ○ Δ Δ 2 A-1 0.015 B-1 0.0375 C-PB 4D-2 0.5 3500 ○ ○ ○ 3 A-2 0.015 B-1 0.0375 C-PB 4 D-2 0.5 3500 ○ ○ ○ 4A-3 0.015 B-1 0.0375 C-PB 4 D-2 0.5 3500 ○ ○ ○ 5 A-3 0.015 B-1 0.0375C-PB 4 D-2 0.5 35000 ⊚ ○ ⊚ 6 A-3 0.015 B-1 0.0375 C-PB 4 D-2 0.5 51600 ⊚○ ⊚ 7 A-4 0.015 B-1 0.0375 C-PB 4 D-2 0.5 3500 ⊚ ○ ○ 8 A-4 0.015 B-10.0375 C-PB 4 D-2 0.5 51600 ⊚ ○ ⊚ 9 A-1 0.015 B-2 0.0375 C-PB 4 D-2 0.53500 ⊚ ○ ⊚ 10 A-1 0.015 B-1 0.0375 C-PB 4 D-2 0.2 3500 ⊚ ○ ○ 11 A-40.015 B-2 0.0375 C-PB 4 D-2 0.5 3500 ⊚ ○ ⊚ 12 A-1 0.015 B-1 0.0375 C-PB2 D-2 0.2 3500 ⊚ ○ ⊚ 13 A-1 0.015 B-2 0.0375 C-PB 2 D-2 0.2 3500 ⊚ ⊚ ⊚14 A-2 0.015 B-2 0.0375 C-PB 2 D-2 0.2 3500 ⊚ ⊚ ⊚ 15 A-3 0.015 B-20.0375 C-PB 2 D-2 0.2 3500 ⊚ ⊚ ⊚ 16 A-3 0.015 B-2 0.0375 C-PB 2 D-2 0.23500 ⊚ ○ ⊚ 17 A-3 0.015 B-2 0.0375 C-PB 2 D-2 0.2 3500 ⊚ ○ ○ 18 A-40.015 B-2 0.0375 C-PB 2 D-2 0.2 3500 ⊚ ⊚ ⊚ 19 A-1 0.015 B-1 0.0375 C-PB2 D-2 0.2 3500 ○ ○ ○ 20 A-4 0.015 B-2 0.0375 C-PB 2 D-2 0.2 3500 ⊚ ○ ⊚Com- 1 A-1 0.015 B-1 0.0375 C-PB 4 D-2 0.5 126 ○ Δ × parative 2 A-20.015 B-1 0.0375 C-PB 4 D-2 0.5 126 ○ Δ × Example 3 A-3 0.015 B-1 0.0375C-PB 4 D-2 0.5 126 ○ Δ × 4 A-4 0.015 B-1 0.0375 C-PB 4 D-2 0.5 126 ○ Δ ×5 A-1 0.015 B-2 0.0375 C-PB 2 D-2 0.2 126 ○ ○ × 6 A-2 0.015 B-2 0.0375C-PB 2 D-2 0.2 126 ○ ○ × 7 A-3 0.015 B-2 0.0375 C-PB 2 D-2 0.2 126 ○ ○ ×8 A-4 0.015 B-2 0.0375 C-PB 2 D-2 0.2 126 × × × 9 A-1 0.015 B-1 0.0375C-PB 2 D-2 0.2 126 Δ × × 10 A-4 0.015 B-2 0.0375 C-PB 2 D-2 0.2 126 × ××

TABLE 2 Catalyst composition for hydrogenation (C) (D) Evaluationresults Mass Mass Rate of ratio ratio Shearing hydrogenating polymerFilter (A) (B) to (A) to (A) rate Initial After clogging in Type (mmol)Type (mmol) Type (−) Type (−) (1/s) stage 30 days extruder Example 21A-1 0.015 B-1 0.0375 C-1 2 — — 3500 ○ Δ ○ 22 A-1 0.015 B-1 0.0375 C-1 2D-1 0.5 3500 ○ ○ ○ 23 A-3 0.015 B-1 0.0375 C-1 2 D-1 0.5 3500 ○ ○ ○ 24A-3 0.015 B-1 0.0375 C-1 2 D-1 0.5 35000 ⊚ ○ ⊚ 25 A-4 0.015 B-1 0.0375C-1 2 D-1 0.5 3500 ○ ○ ○ 26 A-4 0.015 B-1 0.0375 C-1 2 D-1 0.5 51600 ⊚ ○○ 27 A-1 0.015 B-1 0.0375 C-1 4 D-1 0.5 3500 ○ Δ ○ 28 A-1 0.015 B-20.0375 C-1 2 D-1 0.5 3500 ⊚ ○ ⊚ 29 A-1 0.015 B-2 0.0375 C-1 2 D-1 0.53500 ⊚ ○ ○ 30 A-1 0.015 B-2 0.0375 C-1 2 D-1 0.5 3500 ○ ○ ○ 31 A-1 0.015B-1 0.0375 C-2 2 D-1 0.5 3500 ○ Δ ○ 32 A-1 0.015 B-2 0.0375 C-3 2 D-10.5 3500 ○ ○ ⊚ 33 A-1 0.015 B-1 0.0375 C-1 2 D-2 0.5 3500 ⊚ ○ ○ 34 A-40.015 B-2 0.0375 C-1 2 D-2 0.5 3500 ⊚ ○ ⊚ 35 A-1 0.015 B-1 0.0375 C-1 2D-1 0.5 3500 ○ Δ ○ 36 A-4 0.015 B-2 0.0375 C-1 2 D-2 0.5 3500 ⊚ ○ ○Comparative 11 A-1 0.015 B-1 0.0375 C-1 2 — — 126 Δ × × Example 12 A-10.015 B-1 0.0375 C-1 2 D-1 0.5 126 ○ Δ × 13 A-4 0.015 B-1 0.0375 C-1 2D-1 0.5 126 ○ Δ × 14 A-1 0.015 B-1 0.0375 C-1 2 D-1 0.5 126 Δ Δ × 15 A-40.015 B-2 0.0375 C-1 2 D-2 0.5 126 × × ×

It is to be noted that components (A) ((A-1) to (A-4)), components (B)((B-1) and (B-2)), components (C) ((C-PB) and (C-1) to (C-3)), andcomponents (D) ((D-1) and (D-2)) in Table 1 and Table 2 are as follows.

Components (A)

-   (A-1): Bis(η(5)-cyclopentadienyl)titanium di(p-tolyl)-   (A-2): Bis(η(5)-cyclopentadienyl)titanium di(phenyl)-   (A-3): Bis(η(5)-cyclopentadienyl)titanium di(3,4-xylyl)-   (A-4): Bis(η(5)-1,3-dimethylcyclopentadienyl)titanium dichloride

Components (B)

-   (B-1): Triethyl aluminum-   (B-2): sec-Butyl lithium

Components (C)

-   (C-PB): Polybutadiene-   (C-1): Myrcene-   (C-2): Isoprene-   (C-3): 1,7-Octadiene

Components (D)

-   (D-1): Tetrahydrofuran-   (D-2): N,N,N′,N′-tetramethylethylenediamine

It was found that, when the catalyst compositions for hydrogenationproduced in Examples 1 to 36 were used, these compositions had highactivity of hydrogenation, and the degree of filter clogging in anextruder upon the production of a hydrogenated polymer could be reduced.

The present application is based on Japanese patent applications(Japanese Patent Application No. 2012-235006) and (Japanese PatentApplication No. 2012-235009) filed with the Japan Patent Office on Oct.24, 2012; the disclosure of which is hereby incorporated by reference.

INDUSTRIAL APPLICABILITY

The catalyst composition for hydrogenation obtained by the method forproducing a catalyst composition for hydrogenation of the presentinvention has industrial applicability as a catalyst composition forhydrogenation, which is used in a hydrogenation step for producing ahydrogenated polymer compound used as a modifier for polypropylene orpolyethylene.

1. A method of producing a catalyst composition for hydrogenation,wherein: (A): a titanocene compound represented by following generalformula (1):

(wherein R⁵ and R⁶ each represent a group selected from the groupconsisting of hydrogen, a hydrocarbon group having 1 to 12 carbon atoms,an aryloxy group, an alkoxy group, a halogen group and a carbonyl group,and may be the same or different; and R¹ and R² represent a groupselected from the group consisting of hydrogen and a hydrocarbon grouphaving 1 to 12 carbon atoms, and may be the same or different; providedthat R¹ and R² are not all hydrogens or all hydrocarbon groups having 1to 12 carbon atoms); (B): a compound containing at least one elementselected from the group consisting of elements Li, Na, K, Mg, Zn, Al,and Ca; and (C): an unsaturated compound are used, and the methodcomprises: a force application step of applying a shearing force at ashearing rate of 1000 (1/s) or more to at least the (A); and a step ofmixing the (A), the (B), and the (C).
 2. The method of producing thecatalyst composition for hydrogenation according to claim 1, wherein the(C) is an unsaturated polymer (C1) having a fraction of an olefinicunsaturated double bond content of the side chains based on a totalolefinic unsaturated double bond content of 0.25 to 1.0.
 3. The methodof producing the catalyst composition for hydrogenation according toclaim 1, wherein the (C) is an unsaturated compound (C2) having amolecular weight of 400 or less.
 4. The method of producing the catalystcomposition for hydrogenation according to claim 1, wherein a mass ratioof the (C) to the (A) ((C)/(A)) is set in a range of 0.1 to
 8. 5. Themethod of producing the catalyst composition for hydrogenation accordingto claim 1, wherein a mass ratio of the (C) to the (A) ((C)/(A)) is setin a range of 0.1 to
 4. 6. The method of producing the catalystcomposition for hydrogenation according to claim 1, wherein the (C) isan unsaturated polymer (C1) having a fraction of an olefinic unsaturateddouble bond content of the side chains based on an olefinic unsaturateddouble bond content of 0.25 to 1.0, and a mass ratio of the (C1) to the(A) ((C1)/(A)) is set in a range of 0.3 to
 8. 7. The method of producingthe catalyst composition for hydrogenation according to claim 1comprising: the step of mixing the (A) and the (B) after the forceapplication step.
 8. The method of producing the catalyst compositionfor hydrogenation according to claim 7: the step of mixing after the (B)is added to a mixture of the (A) and the (C), after the forceapplication step.
 9. The method of producing the catalyst compositionfor hydrogenation according to claim 8 comprising: the step of mixingthe (A), the (B), and the (C) after the (B) is added to the mixture ofthe (A) and the (C), after or during the force application step ofapplying a shearing force at a shearing rate of 1000 (1/s) or more to amixture of the (A) and the (C).
 10. The method of producing the catalystcomposition for hydrogenation according to claim 1, further comprising astep of mixing a polar compound (D), wherein a mass ratio of the (D) tothe (A) ((D)/(A)) is set in a range of 0.01 to
 2. 11. The method ofproducing the catalyst composition for hydrogenation according to claim1, further comprising a step of mixing a polar compound (D), wherein amass ratio of the (D) and the (A) ((D)/(A)) is set in a range of 0.01to
 1. 12. The method of producing the catalyst composition forhydrogenation according to claim 1, wherein the (B) is an organiclithium compound.
 13. The method of producing the catalyst compositionfor hydrogenation according to claim 1, wherein a conjugated dienepolymer, or a copolymer formed of a conjugated diene and a vinylaromatic hydrocarbon is used as the unsaturated compound (C).
 14. Acatalyst composition for hydrogenation obtained by the method ofproducing the catalyst composition for hydrogenation according toclaim
 1. 15. The method of producing the catalyst composition forhydrogenation according to claim 4 comprising: the step of mixing the(A), the (B), and the (C) after the (B) is added to the mixture of the(A) and the (C), after or during the force application step of applyinga shearing force at a shearing rate of 1000 (1/s) or more to a mixtureof the (A) and the (C).
 16. The method of producing the catalystcomposition for hydrogenation according to claim 6 comprising: the stepof mixing the (A), the (B), and the (C) after the (B) is added to themixture of the (A) and the (C), after or during the force applicationstep of applying a shearing force at a shearing rate of 1000 (1/s) ormore to a mixture of the (A) and the (C).
 17. The method of producingthe catalyst composition for hydrogenation according to claim 16,further comprising a step of mixing a polar compound (D), wherein a massratio of the (D) to the (A) ((D)/(A)) is set in a range of 0.01 to 2.